Regenerable battery for electricity generation from gas separation process of captured carbon dioxide

ABSTRACT

The invention pertains to processes for separating gases, acid gas, hydrocarbons, air gases, or combinations thereof. The processes may employ using a liquid phase cloud point with or without subsequent liquid-liquid separation. In some embodiments membranes can be employed with reverse osmosis to regenerate a solvent and/or an antisolvent. In some embodiments thermal switching phase changes may be employed during absorption or desorption to facilitate separation.

CROSS REFERENCE TO RELATED APPLICATIONS

The instant application is a continuation of U.S. Ser. No. 16/226,182, filed Dec. 19, 2018, which is a continuation-in-part of U.S. Ser. No. 15/424,218 filed Feb. 3, 2017, which claims priority to U.S. Ser. No. 62/290,519 filed Feb. 3, 2016 and U.S. Ser. No. 62/309,666 filed Mar. 17, 2016 and 62/325,620 filed Apr. 21, 2016 and 62/363,445 filed Jul. 18, 2016 and 62/375,471 filed Aug. 16, 2016. The instant application also claims priority to U.S. Ser. No. 62/760,155 filed Nov. 13, 2018 and U.S. Ser. No. 62/734,398 filed Sep. 21, 2018. This application is also related to PCT/US2015/064669 filed Dec. 9, 2015 claiming priority to U.S. Ser. No. 14/826,771 filed Aug. 14, 2015 which is now U.S. Pat. No. 9,624,111 and which claims priority to U.S. Serial Nos. 62/106,822 filed Jan. 23, 2015 and 62/090,272 filed Dec. 10, 2014 and 62/159,481 filed May 11, 2015. This application is also related to U.S. Ser. No. 15/476,494 filed Mar. 31, 2017 which is currently allowed and was a divisional of U.S. Ser. No. 14/826,771 filed Aug. 14, 2015 which is now U.S. Pat. No. 9,624,111. All the aforementioned applications are incorporated herein by reference for U.S. purposes.

BACKGROUND AND SUMMARY OF INVENTION

Among human activities, CO₂ emissions from electricity generation and industry make up 65% of global greenhouse gas emissions. Considering the world's growing energy demand and continued dependence on fossil fuels, there is an unprecedented need to develop technologies to significantly reduce CO₂ emissions.

One promising means of reducing CO₂ emissions is post-combustion CO₂ capture and utilization (CCU), which transforms low concentrations of CO₂ in emissions into high purity CO₂ for utilization or disposal. However, implementation of these technologies, such as the chilled ammonia and monoethanolamine (MEA) carbon capture processes, has been limited to pilot plants due to enormous operating costs. The most effective prior art processes require elevated temperature heat, generally supplied by steam diverted from power generation, increasing electricity costs by over 70% in some cases. Elevated temperature heat constitutes >80% of the energy consumption in current carbon capture processes and is the costliest component of CO₂ capture. A significantly lower operating and capital cost CO₂ capture system is necessary to make CCU an effective means of reducing CO₂ emissions.

Another means of reducing CO₂ emissions is pre-combustion CO₂ capture. Pre-combustion CO₂ capture involves removing the carbon or carbon dioxide from fuel before combustion is completed. For example, pre-combustion CO₂ capture may involve transforming natural gas and water into hydrogen and CO₂ using steam reforming and water gas shift reaction, and subsequently separating said CO₂ from said hydrogen before employing said hydrogen as a fuel. Pre-combustion CO₂ capture, as well as other applications for acid gas separation, including, for example, CO₂ separation from natural gas or biogas, employ separation technologies based on physical absorption, chemical absorption, gas phase membrane separation, or adsorption. Physical absorption CO₂ separation technologies involve pressurized absorption of CO₂ into an inert solvent, such as water or an organic solvent, then the desorption of CO₂ under reduced pressure conditions, often with the application of heat. Prior art physical absorption CO₂ separation technologies consume significant electricity in the compression or pressurization of the acid gas laden gas stream and the electricity required to pump the relatively substantial amounts of liquid throughout the separation process. Current physical absorption CO₂ separation technologies absorb acid gas in the same liquid reagent composition and liquid phase as they desorb acid gas. As a result, a trade-off occurs—the more soluble acid gas is in a physical solvent, the more energy that is required during desorption to regenerate the physical solvent; the less soluble acid gas is in a physical solvent, the more energy that is required during the pressurization/compression during absorption. Furthermore, in prior art technologies, solubility change or absorption or desorption almost entirely driven by changing the partial pressure and/or temperature of a liquid, while the solubility parameters or properties of the liquid itself remain unchanged.

Pure CO₂ is a valuable product with 80 Mt per year commercial market. Due to the cost prohibitive nature of current CO₂ capture systems, over 80 percent of the demand for pure CO₂ is supplied by the unsustainable drilling of CO₂ source fields, which contain CO₂ that has been sequestered for millions of years. An effective system that captures CO₂ from flue gas below market prices would at least partially displace the pure CO₂ production from these unsustainable and counterproductive sources.

Advantageously, the present invention pertains to new highly efficient, low energy, and low-cost systems and methods to separate gases such as an acid gas (e.g., one comprising CO₂), a basic gas, a hydrocarbon, an inert gas, air, or a combination thereof. In one embodiment the invention involves a process for separating gas comprising absorbing one or more gases in a liquid system comprising one or more physical solvents, wherein said one or more physical solvents comprise one or more liquid phases in the liquid system. The conditions are controlled to change the number and composition of liquid phases in said liquid system. The system may exhibit a phase transition at a lower critical solution temperature, upper critical solution temperature, or both. Said phase transitions may result in a change in the equilibrium solubility or kinetics of absorption or desorption, or combination thereof of one or more gases in one or more liquid phases.

In another embodiment, the invention involves a process for separating gas comprising absorbing a first gas and a second gas with a one phase liquid solution and changing the one phase liquid solution to a second liquid solution comprising two or more phases wherein one phase of the two or more phases is selective for said first gas relative to said second gas.

In another embodiment, the invention involves process for separating gas comprising absorbing a first gas and a second gas with a liquid solution comprising two or more phases and transforming the two-phase liquid solution to a second liquid solution comprising one phase wherein the second liquid solution is selective for dissolving said first gas relative to said second gas.

In another embodiment, the invention involves a process for separating gas comprising absorbing one or more gases with a liquid solution comprising one or more physical solvents; mixing an antisolvent with said liquid solution to form a second liquid solution; desorbing at least one gas from said second liquid solution; and treating at least a portion of said second liquid solution with one or more membranes to separate antisolvent from said one or more physical solvents. These and other embodiments are described in detail below.

BRIEF DESCRIPTION OF THE DRAWINGS

FIGS. 1A and 1B illustrate specific gas separation embodiments employing a physical solvent with the number of phases changing.

FIGS. 2A and 2B illustrate specific gas separation embodiments employing a physical solvent with the number of phases changing.

FIGS. 3A and 3B illustrate specific gas separation embodiments employing a physical solvent with the number of phases changing.

FIG. 4 illustrates a specific gas separation embodiment employing a gas absorbing solvent with the number of phases changing.

FIG. 5 illustrates a specific gas separation embodiment employing a gas absorbing solvent with the number of phases changing.

FIGS. 6A and 6B illustrate specific gas separation embodiments employing a gas absorbing solvent and mild basic or acidic conditions.

FIGS. 7A and 7B and 7C illustrate specific gas separation embodiments employing a heat exchanger or heat pump.

FIG. 8 illustrates specific gas separation embodiments wherein two or more gases are absorbed in a single liquid phase.

FIGS. 9A and 9B and 9C illustrate specific gas separation embodiments using a physical solvent, antisolvent, and membrane.

FIGS. 10A and 10B and 10C illustrate specific gas separation embodiments using systems and methods for active cloud point adjustment.

FIGS. 11A and 11B and 11C illustrate specific gas separation embodiments using systems and methods for active cloud point adjustment.

FIG. 11D is a representative production process with pressure retarded osmosis.

FIG. 12 is a representative production process with a copper battery.

FIG. 13 is a representative production process with a low grade heat source.

FIG. 14 shows an ammonium/ammonia ratio as a function of pH.

DETAILED DESCRIPTION OF THE INVENTION Gas Separation—General Processes

In some embodiments the present invention pertains to systems and processes for separating gases such as acid gases. In one embodiment the process involves absorbing one or more gases in a liquid system comprising one or more physical solvents. A physical solvent is generally a solvent that does not chemically react with the gas or gases being absorbed. The physical solvents employed may vary depending upon the gases to be absorbed, the conditions employed, other steps, and desired results. Suitable physical solvents may include, for example, an organic solvent, an organic polymer, or a combination thereof. The temperature and pressure of the absorbing step may vary depending upon the other conditions and the ingredients. Generally, room temperature and pressure or higher is suitable, although other temperatures and pressures may also be suitable depending upon solvent(s) and desired results.

Next, the conditions of the liquid system are controlled or modified to change the number and composition of liquid phases in said liquid system. That is, the number of liquid phases may change from one phase to two or more phases. Alternatively, or additionally, a two or more-phase system may be reduced to one phase. Similarly, the composition in the various liquid phases may change.

The change in number and composition of liquid phases may be accomplished in any convenient manner. Typically, the controlled conditions of the liquid system involve employing conditions such that the system pass through a critical solution temperature, e.g., a lower critical solution temperature, upper critical solution temperature, or both, to accomplish the desired change in number and composition of liquid phases. These changes in phases and compositions may occur before, during, or after said absorbing step. In one embodiment, during said absorbing step the liquid system changes phases at a lower critical solution temperature wherein at least a portion of any heat generated is absorbed by the endothermic phase change. At least a portion of any heat generated may be recovered in any convenient manner. For example, following said endothermic phase change into two or more liquid phases, said heat may be released prior to or during a subsequent desorbing step, wherein the two or more liquid phases undergo an exothermic phase change into a single liquid phase. In some instances, it may be desirable to include a separation step prior to and/or after the absorbing step or desorbing step. Liquid phases may be separated and/or undergo purification or treatment prior to or after absorption. Gases may be separated and/or purified prior to or after absorption or desorption.

In another embodiment the liquid system may change from two or more liquid phases to one liquid phase, for example, at or below one or more LCSTs or at or above one or more UCSTs. Said formation of one liquid phase from two or more liquid phases may occur, for example, prior to or during the desorption or absorption of one or more gases. Said formation of liquid phase from two or more liquid phases may facilitate said absorbing or desorbing. In the case of desorbing, said formation of one liquid phase from two or more liquid phases may occur in a manner such that (1) the solubility of one or more gases is reduced; (2) the partial pressure of one or more gases increased; (3) heat results to facilitate desorption; (4) the solubility of the gas to be desorbed is decreased relative to other absorbed gases; or (5) a combination thereof. In the case of absorbing, said formation of one liquid phase from two or more liquid phases may occur in a manner such that (1) the solubility of one or more gases is increased; (2) the partial pressure of one or more gases is decreased; (3) heat is absorbed to facilitate absorption; (4) the solubility of the gas to be desorbed is decreased relative to other absorbed gases; or (5) a combination thereof. The single liquid phase may be regenerated into two or more liquid phases, for example, by changing one or more conditions such that two or more liquid phases form at or above one or more LCSTs or at or below one or more UCSTs. The two or more liquid phases may be separated or remain as a liquid mixture.

Similarly, in another embodiment the liquid system may change from one liquid phase to two or more liquid phases, for example, at or above one or more LCSTs or at or below one or more UCSTs. Said formation of two liquid phases from one liquid phase may occur, for example, prior to or during the desorption or absorption of one or more gases. Said formation of two or more liquid phases from one liquid phase may facilitate said absorbing or desorbing. In the case of desorbing, said formation of two or more liquid phases from one liquid phase may occur in a manner such that (1) the solubility of one or more gases is reduced; (2) the partial pressure of one or more gases increased; (3) heat results to facilitate desorption; (4) the solubility of the gas to be desorbed is decreased relative to other absorbed gases; or (5) a combination thereof. In the case of absorbing, said formation of two or more liquid phases from one liquid phase may occur in a manner such that (1) the solubility of one or more gases is increased; (2) the partial pressure of one or more gases is decreased; (3) heat is absorbed to facilitate absorption; (4) the solubility of the gas to be desorbed is decreased relative to other absorbed gases; or (5) a combination thereof. The single liquid phase may be regenerated into two or more liquid phases, for example, by changing one or more conditions such that two or more liquid phases form at or above one or more LCSTs or at or below one or more UCSTs. The two or more liquid phases may be separated or remain as a liquid mixture.

One or more liquid phases may comprise an antisolvent and one or more liquid phases may comprise a physical solvent. An antisolvent is generally a substance which may change the solubility of or selectivity for one or more gases. Antisolvents employed, if any, will generally vary depending upon the gas or gases, ingredients of the liquid system, and desired results. Antisolvents employed to reduce the solubility of one or more gases may be selected from the group consisting of water, ionic compound, a reagent with a low gas solubility, or a combination thereof. Antisolvents employed to increase the solubility of one or more gases may be selected from the group consisting of water, ionic compound, an organic solvent, a reagent with a high gas solubility, or a combination thereof. In some embodiments antisolvent may be regenerated in a convenient manner. One manner may be to control the conditions such that at least one liquid phase comprises a substantial concentration of the antisolvent.

Other embodiments of the invention may involve separating gas by absorbing a first gas and a second gas with a one phase liquid solution the one phase liquid solution can then be changed or converted or transitioned to a second liquid solution comprising two or more phases wherein one phase of the two or more phases is selective for said first gas relative to said second gas. The one phase liquid solution may comprise one or more physical solvents, if desired. In some cases it may be desirable that one phase of the two or more liquid phases is selected such that it exhibits one or more up to all of the following properties relative to a second phase of the two or more phases (1) higher selectivity for one more gases; (2) higher concentration of one more gases; (3) greater desorption kinetics for one or more gases, (4) greater equilibrium partial pressure of one or more gases, (5) lower energy of regeneration of one or more gases; (6) higher reactivity for one or more gases; (7) higher liquifying ability for one or more gases; (8) higher gas equilibrium partial pressure; (9) faster desorption kinetics for one or more gases; (10) greater desorption capability for one or more gases; (11) lower viscosity; (12) lower volatility; (13) lower degradation (14) lower corrosiveness; (15) higher compatibility with impurities; and (16) fewer total impurities in desorbed gases. Following absorption, the first gas may be desorbed, if desired, in any convenient manner.

In another embodiment, the invention involves a process for separating gas comprising first absorbing a first gas and a second gas with a liquid solution comprising two or more phases. The two-phase liquid solution may then be transformed or converted to a second liquid solution comprising one phase wherein the second liquid solution is selective for dissolving said first gas relative to said second gas.

In yet another embodiment, the invention involves a process for separating gas comprising first absorbing one or more gases with a liquid solution comprising one or more physical solvents. An antisolvent may then be mixed with said liquid solution to form a second liquid solution and at least one gas may be desorbed from said second liquid solution. At least a portion of said second liquid solution may then be treated with one or more membranes to separate antisolvent from said one or more physical solvents. Typical useful membranes may include, for example, membranes that separate by having a molecular weight cutoff while one or more of the physical solvents has a molecular weight below the membrane's molecular weight cutoff. Suitable physical solvents vary depending upon the circumstances but often may include, for example, those selected from the group consisting of water, organic solvent, glycol, carbonate, carbonate ester, ester, ether, diol, lactam, protic solvents, aprotic solvents, amide, alcohol, fluorinated compound, hydrocarbon, organic polymer, alkylene glycol, alkylene carbonate, polyol, urea, and mixtures thereof. If desired, the anti solvent may be mixed with said liquid solution under conditions to modify the pH of the second liquid solution and facilitate desorbing. The antisolvent may work in any number of ways. For example, the antisolvent may modify the solubility of one or more gases relative to the physical solvent alone. For example, the antisolvent may modify the solubility of at least one dissolved gas relative to at least one other different dissolved gas in the second liquid solution. In some embodiments it may be desirable to enrich the antisolvent with one or more dissolved gases relative to the total solubility of said gases in said antisolvent. Typical other useful membranes may include, for example, membranes that separate by having a molecular weight cutoff while one or more of the antisolvents comprises one or more compounds with a molecular weight or hydration radius greater than the molecular weight cutoff of the membrane. Suitable antisolvents may include, for example, those that comprise an organic acid, an inorganic acid, an acid with a hydration radius greater than 80 Daltons, a polymer, an acidic polymer, an ionic compound, an acidic ionic compound, a weak base—strong acid, a cation-hydrogen or dihydrogen-anion or trihydrogen-anion salt, an alkali hydrogen sulfate salt, an ammonium—strong acid salt, a common-ion salt, a citric acid, base, an amine, an imine, an azine, an organic base, an inorganic base, a strong base, a base with a hydration radius greater than 80 Daltons, a polymer, a basic polymer, an ionic compound, a basic ionic compound, a strong base—weak acid, a common-ion salt water, water, an organic solvent or a mixture thereof.

In some cases, it may be desirable that the solubility of one or more gases in the second liquid solution is (1) less than the solubility of one or more gases in the liquid solution or (2) less than the solubility of one or more gases in the antisolvent or (3) combination thereof. In other cases, it may be desirable that the solubility of one or more gases in the second liquid solution is (1) greater than the solubility of one or more gases in the liquid solution or (2) greater than the solubility of one or more gases in the antisolvent or (3) combination thereof. The one or more gases may be any that are capable of being separated by the aforementioned processes. Suitable gases may comprise and acid gas, a basic gas, a hydrocarbon, an inert gas, air, or a combination thereof.

Process Embodiments in FIGS. 1-9

FIG. 1A: A gas separation embodiment employing a physical solvent with LCST or UCST phase change wherein the physical solvent undergoes endothermic phase change, such as forming less or more liquid phases, in the absorber, absorbing a portion of the heat of absorption. The embodiment may further comprise releasing said absorbed heat through the reverse exothermic phase change in the desorber. The present figure undergoes endothermic LCST phase change in the absorber, forming two or more liquid phases, and undergoes an exothermic dissolution LCST phase change in the desorber, forming a single liquid phase or less liquid phases or smaller liquid phases.

FIG. 1B: A gas separation embodiment employing a physical solvent with a UCST phase change wherein the physical solvent is cooled to form two or more liquid phases at or below a UCST and gas is absorbed into the two or more liquid phases in the absorber. The embodiment further comprises heating said two or more liquid phases at or above a UCST temperature, resulting in the dissolution of the two or more liquid phases into, for example, a single liquid phase. The solubility of one or more gases may be greater in the two or more liquid phases than in the combined single liquid phase solution, further facilitating gas partial pressure swing. If desired, heat may be applied, for example, during desorption. If desired, the embodiment may undergo, including, but not limited to, desorption using heat or without a carrier gas or using the desorption methods described in, for example, FIG. 2B, or a combination thereof.

FIG. 2A: A gas separation embodiment employing a physical solvent with a LCST phase change wherein gas is absorbed one of the two at least partially separated liquid separated liquid phases originating from a LCST phase change. The ‘gas-rich’ phase is mixed with the other liquid phase before or, if employed, within the desorber. The combined solution may, for example, have a lower solubility of gas than the liquid phase employed in gas absorption. The present embodiment may employ, for example, air stripping or other carrier gas stripping to facilitate the desorption of one or more dissolved gases.

FIG. 2B: An embodiment similar to FIG. 2A, except the present embodiment may employ heat input, depressurization, or a combination thereof to desorb dissolved gas. Additionally, the present embodiment may form pure or relatively separated desorbed gas using, for example, including, but not limited to, flashing, depressurization, or desorption with a condensable, or separable stripping gas, or combination thereof.

FIG. 3A: A gas separation embodiment employing a physical solvent with a LCST phase change wherein gas is absorbed in two or more separated liquid phases originating from a LCST phase change. Said two or more separated liquid phases may be placed in individual absorption columns specific to each liquid phase (for example: Abs #1 and Abs #2). The two or more liquid phases may be mixed or dissolved or combination thereof before or during the desorption of one or more gases.

FIG. 3B: An embodiment similar to FIG. 3A. The present embodiment may employ heat input, depressurization, or a combination thereof to desorb dissolved gas. Additionally, the present embodiment may form pure or relatively separated desorbed gas using, for example, including, but not limited to, flashing, depressurization, or desorption with a condensable or separable stripping gas, or combination thereof.

FIG. 4: A gas separation embodiment employing a gas absorbing solvent with a UCST phase change. The embodiment may comprise, for example, cooling a UCST solvent at or below its UCST and at least partially separating the resulting two or more liquid phases. The embodiment may further comprise absorbing one or more gases into one of said at least partially separated liquid phases. The embodiment may further comprise combining said two or more liquid phases and desorbing gases from the resulting combined mixture or solution, the application of heat, the presence of a stripping gas, or a combination thereof.

FIG. 5: A gas separation embodiment employing a gas absorbing solvent with a UCST phase change. The embodiment may comprise, for example, cooling a UCST solvent at or below its UCST and separating the resulting two or more liquid phases. The embodiment may further comprise transferring said two or more liquid phases into separate absorption columns and absorbing one or more gases into one or more of said separated liquid phases. The embodiment may further comprise desorbing said one or more gases from said one or more liquid phases or a mixture or combined solution of said liquid phases. For example, the present embodiment may involve combining said two or more liquid phases and desorbing gases from the resulting combined mixture or solution, the application of heat, the presence of a stripping gas, or a combination thereof.

FIG. 6A: A gas separation embodiment employing a gas absorbing solvent comprising a mildly basic or acidic solution. The mildly basic or acidic solution may possess greater absorption capacity of acid gases or basic gases, respectively, than, for example, water. However, the mildly basic or acidic solution may function similarly to a conventional physical solvent in that, for example, it has relatively weak interactions with said acidic or basic gases. If desired, it may not possess a metathesis or displacement reaction with said acidic or basic gases and, for example, may have stronger affinity for its current anion or cation than the one or more anions or cations associated with said acidic or basic gases, respectively. The present embodiment may employ air stripping or carrier gas stripping of the one or more absorbed gases.

FIG. 6B: An embodiment similar to FIG. 6A, except employs heat input, depressurization, or a combination thereof to desorb one or more dissolved gases. Additionally, the present embodiment may form pure desorbed gas through flashing, through depressurization, or desorption with a condensable or separable stripping gas.

FIG. 8: Systems & Methods for Gas Separation Comprising Selective Gas Separation Wherein Two or More Gases are Absorbed in a Single Liquid Phase Solution. The present embodiment may further comprise LCST or UCST phase change of the combined solution into two or more liquid phases. The present embodiment may further comprise wherein at least one or more of said liquid phases are selective for desorption of one or more of said absorbed gases.

FIG. 9A: Systems & Methods for Gas Separation comprising 1) a physical solvent for absorption of one or more gases, 2) an antisolvent, which when mixed with said physical solvent reduces the solubility of one or more gases relative to the physical solvent alone, 3) a semi-permeable membrane which separates at least a portion of said physical solvent from said antisolvent to, for example, regenerate the process. The present embodiment may, for example, employ an absorption column to absorb one or more gases and a desorption column or unit to desorb said one or more gases from, for example, the combined physical solvent+antisolvent solution. The present embodiment may desorb one or more gases as pure gases or using carrier gas stripping or air stripping.

FIG. 9B: An embodiment similar to FIG. 9A, except employs two separate absorbers or gas contactors, wherein one absorber enriches the physical solvent solution with one or more gases and another absorber enriches the antisolvent with one or more gases. Although the antisolvent may possess lower or significantly lower solubility of one or more gases than the physical solvent, it may be desirable to enrich the antisolvent with one or more gases before mixing to minimize, for example, dilutive effects of the antisolvent.

FIG. 9C: An embodiment similar to FIG. 9B, except the present embodiment may employ heat input, depressurization, or a combination thereof to desorb dissolved gas. Additionally, the present embodiment may form pure or relatively separated desorbed gas through flashing, through depressurization, or desorption with a condensable or separable stripping gas.

FIG. 10A: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more UCST phase transitions. FIG. 10A may show the present embodiment undergoing active liquid system cloud point adjustment to, for example, decrease one or more UCSTs.

FIG. 10B: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more UCST phase transitions. FIG. 10B may show the present embodiment undergoing active liquid system cloud point adjustment to, for example, increase one or more UCSTs.

FIG. 10C: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more UCST phase transitions. FIG. 10C may show the present embodiment maintain one or more UCSTs, or composition of liquid phases, or bypassing of permeate addition or membrane-based concentrating, or combination thereof.

FIG. 11A: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more LCST phase transitions. FIG. 11A may show the present embodiment undergoing active liquid system cloud point adjustment to, for example, decrease one or more LCSTs.

FIG. 11B: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more LCST phase transitions. FIG. 11B may show the present embodiment undergoing active liquid system cloud point adjustment to, for example, increase one or more LCSTs.

FIG. 11C: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more LCST phase transitions. FIG. 11C may show the present embodiment maintain one or more LCSTs, or composition of liquid phases, or bypassing of permeate addition or membrane-based concentrating, or combination thereof.

SPECIFIC EMBODIMENTS OF THE GAS SEPARATION/MEMBRANE SEPARATION/COOLING CLOUD POINT REAGENTS/HEATING CLOUDING POINT REAGENTS PHYSICAL OR PHYSIO-CHEMICAL SOLVENT PROCESSES

Described below are representative specific embodiments of the above general gas separation process that often involves changing the number and composition of liquid phases in a liquid system, as well as, other processes of the invention. 1) The upper or lower critical solution temperature may also be referred to as a cloud point which is generally the point at which a liquid system undergoes a change such as a change in the composition of a phase and/or number of phases, which may also be referred to as switching, e.g., thermal switching, or a transition, e.g., liquid phase transition, or phase change, e.g., liquid phase change, or clouding-out, e.g. the solution clouding-out, or a combination thereof. A UCST phase transition into two or more liquid phases may also be referred to as a ‘cooling’ cloud point or UCST ranges or cloud point temperature range or phase transition temperature range. A LCST phase transition into two or more liquid phases may also be referred to as a ‘heating’ cloud point or cloud point temperature range or phase transition temperature range. Alternatively, phase transition solutions may be referred to as solutions exhibiting ‘condition sensitive solubility change.’ 2) A liquid mixture with more than one liquid phase may be referred to as, including, but not limited to, a multiphasic liquid solution, multiphase liquid solution, multiphase solution, multi-liquid phase solution, biphasic solution, a ‘cloudy’ solution, multiphasic liquid mixture, multiphase mixture, multiphase liquid mixture, a multi-liquid phase mixture, biphasic mixture, biphasic liquid mixture, bilayer mixture, multilayer mixture, multi-liquid phase state, multiphase liquid state, or a combination thereof 3) The dissolution of one or more liquid phases in one or more other liquid phases to form a combined single liquid phase solution or a solution with a different number or composition or both of liquid phases may be referred to as ‘combining’ or ‘dissolution’ or ‘mutually dissolve’ or ‘dissolve’ or ‘combine’ or ‘mixing.’ 4) The mixture of two or more separate liquid phases may also occur without or with minimal dissolution of the liquid phases, which may be referred to as ‘mixing’ or ‘combining’ or ‘merging’ or forming one or more of the example descriptors in ‘2)’. 5) Physical absorbents, media which absorbs one or more gases via physical phenomena or physical interactions, may be referred to as a physical solvent, solvent, physical absorbent solvent, liquid, or a combination thereof 6) A ‘desired gas’ may comprise, for example, a gas is desired to dissolve in the physical solvent or a gas that is desired to be separated from one or more other gases. In some instances, one or more dissolved gases may comprise the desired gas or gases. 7) Separation of one or more liquid phases from one or more other liquid phases in a mixture comprising two or more liquid phases may be referred to as, including, but not limited to, liquid-liquid separation, or separation of liquid phases, or liquid phase separation, phase separation, separating said liquid phases, or a combination thereof. 8) Isolated gas or a gas which has been, at least in part, separated from other gases, may comprise for example, ‘captured gas’ or ‘relatively pure gas’ or ‘pure gas’ or a combination or derivative thereof. 9) ‘Permeate’ or permeate liquid may comprise liquid which passes through one or more semi-permeable membranes or was not or was minimally rejected by one or more semipermeable membranes. ‘Permeate equivalent liquid’ or liquid equivalent to permeate may comprise a liquid with similar composition or characteristics to one or more permeate liquids, however may not have originated, in whole or in part, from a permeate solution resulting from the separation of one or more or a combination of reagents in a liquid system using a semipermeable membrane. 10) Desired gases and dissolved gases may be used interchangeably. Dissolved gases may include gases which may or may not be desired to be separated. 11) Relatively low solubility of one or more gases may mean a liquid with lower total solubility of one or more gases than the solubility of said one or more gases in one or more other liquids in a liquid system. An antisolvent may have, for example, one of the or the lowest solubility of one or more gases relative to the solubility of said gases in other liquid phases in a liquid system. 12) Relatively high solubility of one or more gases may mean a liquid with higher total solubility of one or more gases than the solubility of said one or more gases in one or more other liquids in a liquid system. A physical solvent may have, for example, one of the or the greatest solubility of one or more gases relative to the solubility of said one or more gases in other liquid phases in a liquid system. 13) A liquid or solution ‘rich’ in one or more gases may be a solution with a greater dissolved concentration of said one or more gases than said liquid or solution at another point in a process. A liquid or solution ‘lean’ in one or more gases may be a solution with a lower dissolved concentration of said one or more gases than said liquid or solution at another point in a process. Absorbing a gas or gases in a liquid solution, liquid mixture, or phase may simply mean dissolving the gas or gases. Similarly, when referring to desorbing a gas or gases it is simply meant that the absorbed or dissolved gas or gases is removed in some manner regardless of its form. That is, the absorbed or dissolved gas or gases may be desorbed in the form of a gas or gases or liquid or liquids. If desorbed, for example, as a liquid or liquid phase, said liquid phase may be separated from one or more other liquids using one or more liquid separation methods, which may include, but is not limited to, decanting, and/or may undergo treatment or purification. Before or during absorption or desorption, one or more of said gas or gases may, in part, condense as a liquid.

Summary FIG. 1A:

An embodiment comprising an absorption unit which may recover a portion of the enthalpy of absorption and may ‘cool’ the absorption solution before or during absorption through, for example, the endothermic formation of a multi-liquid phase solution from a single liquid phase solution during absorption. The multiphasic solution may remain ‘cloudy’ during the transfer to the stripper. The embodiment further may comprise a desorption unit, wherein, for example, desorption is facilitated by the exothermic dissolution of the multi-liquid phase solution, forming a liquid solution of different phase composition or a single liquid phase solution. The embodiment may be a drop-in improvement technology as it may be employed as a replacement of pre-existing physical solvent absorber—stripper units.

The embodiment shown in FIG. 1A is a gas, acid gas, hydrocarbon, or combination thereof separation technology. The embodiment shown in FIG. 1A may recover a portion or substantial portion of the heat from the enthalpy of absorption during the absorption of one or more gases or from another heat source and release a portion of or substantial portion said heat during desorption. This capability may also enable the technology to maintain a cooler absorber without external cooling of the absorber and may enable a heat and entropy release during desorption, accelerating desorption kinetics and may create a swing in the equilibrium partial pressure or solubility of one or more gases. The liquid phase transition into two or more liquid phases in, for example, the absorber may enable the absorber to operate with a small or almost non-existent temperature profile between the top of the absorber and the exiting rich solution due to, for example, the latent heat of the endothermic thermal switching. This may enable greater absorption efficiency and less cooling or no parasitic cooling requirement in the solution entering the absorber. The enthalpy of absorption may be recovered by the thermal switching of a solvent during the absorption of one or more gases into the physical absorbent. The temperature increase or the heat of absorption or increase in one or more dissolved gas concentration or a combination thereof may result in the formation of two of more liquid phases, generally forming a multi-liquid phase liquid mixture. Additionally, one or more gases may be more soluble in the multi-liquid phase mixture than in the single liquid phase solution, enabling, for example, significant absorption capacity during absorption in the multi-liquid phase mixture, and equilibrium swing to lower gas solubility during desorption due to, for example, the formation of a single liquid phase solution from a multi-liquid phase mixture.

The present embodiment may be a drop-in technology. For example, the present embodiment may operate within a pressurized absorber, depressurized desorber process configuration, enabling low CAPEX and retrofit to, for example, water or organic physical solvent process. Retrofit may be as simple as replacing water or organic physical solvent with the LCST physical solvent in the present embodiment.

Summary FIG. 1B:

An embodiment where the gas lean single liquid phase solution is cooled below its one or more UCSTs to form a multi-liquid phase solution, for example, before absorption. One or more gases may be absorbed into the multi-liquid phase solution, forming, for example, an acid gas-rich multi-liquid phase solution. The resulting gas rich solution may be subsequently heated and/or mixed to form a single liquid phase solution and may be stripped of the previously absorbed gases. Alternatively, said one or more gases may be absorbed into a multi-liquid phase solution, and, for example, said multi-liquid phase solution dissolves to form a different composition of liquid phases or a single liquid phase solution. Said mutually dissolving may be endothermic and may absorb, for example, a portion of the heat of absorption of one or more gases, and/or provide cooling during absorption.

The present embodiment may benefit from multiple driving forces. During absorption, relatively greater absorption capacity may be driven by, for example, including, but not limited to, the relatively cold temperature of the liquids and/or a greater equilibrium solubility of one or more gases in said multi-liquid phase mixture than said single liquid phase combined solution. Driving forces to facilitate the desorption of one or more dissolved gases may include, but are not limited to, relatively higher temperature than absorption, a relatively lower solubility of one or more gases in the combined single liquid phase solution than the multiphase liquid solution, or the entropy released during the mutual dissolution of the multiphase liquid into a single-phase liquid, or a combination thereof.

The embodiment may be a drop-in technology. If implemented as a drop-in technology or retrofit, depending on the pre-existing equipment, cooling before or during absorption and heating before or during desorption may already exist or may need to be added to a pressurized absorption, depressurized desorption process configuration.

The embodiment shown in FIG. 1B, along with other embodiments described herein, may comprise a gas, acid gas, basic gas, hydrocarbon, or combination thereof separation technology. In the present embodiment, the liquid phase transition may be complementary with the use of external cooling or heating input, as, for example, the multi-liquid phase may remain at said multi-liquid phase state with additional cooling and said single liquid phase combined solution may remain as a single liquid phase with additional heating. The present embodiment may benefit from the difference in solubility of one or more gases in the multi-liquid phase state compared to the single-liquid phase state, while also, for example, being able to benefit from a temperature swing between absorption and desorption. The present embodiment may employ a solution that forms a multi-liquid phase solution while cooling below one or more UCSTs and form a single-phase solution or a lesser multiphase solution while heating above one or more UCSTs. Heating and cooling sources may be ambient or waste heat source, or may be parasitic sources, for example a heat pump or steam, or may comprise one or more heating or cooling sources described herein or known in the art.

Example Inputs and Outputs FIG. 1A

Example INPUTS Example OUTPUTS Acid Gas Laden Gas (G-1 and G-2) Acid Gas-Rich Air (G-5) or Air or Other Acid-Gas Lean Gas captured acid gas (G-4) Acid Gas-Lean Gas (G-3)

Example Inputs and Outputs FIG. 1B

Example INPUTS Example OUTPUTS Acid Gas Laden Gas (G-1 and G-2) Acid Gas-Rich Air (G-5) or Air or Other Acid-Gas Lean Gas captured acid gas (G-4) Acid Gas-Lean Gas (G-3) Electricity (Gas Compressor, Liquid Pumps, Pretreatment Equipment) Heating (H-1) Cooling (CW-1)

Example Step by Step Description FIG. 1A:

-   1. Gas Absorption: One or more or a combination of gas streams (G-1)     is pressurized (Gas Compressor, G-2) and contacted with a desired     gas-lean, single liquid phase solution (L-2), forming a gas stream     lean in one or more gases (G-3) and a desired gas-rich multi-liquid     phase solution (L-1).     -   Note: During absorption, heat may be released, due to, for         example, the enthalpy of absorption, and the concentration of         one or more desired gases may increase in one or more of the         liquid phases. At least a portion of the heat released due to         the heat of absorption may be absorbed due to an endothermic         phase transition of the liquid system from a one liquid phase         solution into a multi-liquid phase mixture. Said endothermic         phase transition may enable a near constant or relatively more         constant temperature profile in the absorption stage. Said         resulting multi-liquid phase solution may have a higher         solubility of one or more desired gases than the initial single         liquid phase solution. -   2. Gas Air Stripping: A multi-liquid phase mixture rich in one or     more desired gases (L-1) may be depressurized and/or transferred to     one or more desired gas desorption or stripping units. In said one     or more desorption of stripping units, L-1 may be contacted with one     or more gases lean in one or more desired gases (G-4), such as air.     One or more desired gases may desorb from the said multi-liquid     phase solution, in which may result in the formation of air rich in     one or more desired gases (G-5) and at least a portion of a single     liquid phase solution lean in one or more desired gases.     -   Desorption/stripping may generally be considered endothermic and         may result in the temperature of the column or flash unit to         decrease. Said temperature decrease may be at or below or pass         through one or more LCSTs of the multi-liquid phase mixture,         resulting in, for example, the exothermic mutual dissolution of         one or more said liquid phases and/or the formation of a single         liquid phase combined solution. A portion of or at least a         portion of said heat may derive from heat absorbed during the         absorption of one or more gases. Said dissolution may also         reduce or eliminate heating demands in the desorber/stripper.         Furthermore, said combined, single phase solution may possess a         lower solubility of one or more gases compared to said         multi-liquid phase mixture, potentially further facilitating         desorption of one or more gases.

Example Step by Step Description FIG. 1B:

-   1. Forming a Multi-Liquid Phase Mixture: A desired gas-lean, single     liquid phase solution (L-4) may be cooled to at or below one or more     UCSTs of the liquid system, which may result in the formation of a     cooled, multi-liquid phase mixture (L-5). -   2. Gas Absorption: One or more or a combination of gas streams     containing one or more desired gases (G-1) may be pressurized (Gas     Compressor, G-2) and contacted with L-5, which may result in the     formation of a gas stream lean in one or more desired gases (G-3)     and a multi-liquid phase mixture rich in one or more desired gases     (L-1) or single liquid phase solution rich in one or more desired     gases (L-2) or a combination thereof -   3. Transition of Multi-Liquid Phase Mixture into a Combined Single     Liquid Phase Solution: A multi-liquid phase mixture rich in one or     more desired gases (L-1) may be heated to at or above one or more     UCSTs, which may result in formation of a single liquid phase     solution (L-3). Said heating may employ using, for example, one or     more heat exchangers (H-1, L-2) and said dissolution may be further     facilitated by mixing in, for example, a static mixer (Static     Mixer). -   4. Desorption     -   a. Gas Air Stripping: A single liquid phase solution rich in one         or more desired gases (L-3) may be depressurized and contacted         with air lean in one or more desired gases (G-4) in, for         example, a gas-liquid contactor. One or more desired gases may         desorb from said single liquid phase solution rich in one or         more desired gases into air lean in one or more desired gases         (G-4), which may form one or more liquid phases lean in one or         more desired gases (L-4) and air rich in one or more desired         gases (G-5).     -   b. Captured Acid Gas Desorption: A single liquid phase solution         rich in one or more desired gases (L-3) may be depressurized         and/or may undergo further heating before or within one or more         desorption units. One or more desired gases may desorb from said         solution rich in one or more desired gases, which may result in         an acid gas-lean liquid solution one or more liquid phases lean         in one or more desired gases and one or more captured gas phase         desired gases or gas streams. Said one or more desired gases or         gas streams may be further treated to remove water vapor or         other contaminants or further separated before, for example,         end-use.

FIG. 1B: Example Performance Driving Forces:

-   -   Equilibrium Solubility Swing: The single liquid phase combined         solution state of the liquid system may possess lower         equilibrium solubility of one or more desired gases relative to         the solubility of said one or more desired gases in a         multi-liquid phase state of the liquid system.     -   Absorption may occur at cooler temperatures: A cooled absorption         solution may be a multi-liquid phase mixture because, for         example, the multi-liquid phase mixture may form from cooling         below one or more UCSTs. Said existence of a multi-liquid phase         liquid mixture in a cooled absorption unit may reduce or         eliminate the need for the separation of one or more liquid         phases or the use of two or more separate absorbers or a         combination thereof.     -   Desorption may occur at higher temperatures     -   Desorption may occur at higher temperatures while receiving the         benefits of the potentially reduced equilibrium solubility from         the combined single liquid phase solution. This may be due to,         for example, the solution forming a single liquid phase from two         or more liquid phases below a certain temperature, enabling, for         example, said solution to be heated while remaining a single         liquid phase solution. As a result, the process may possess the         benefits antisolvent gas solubility reduction (wherein, for         example, on or more of said liquid phases dissolved in said         liquid solution comprises an antisolvent or exhibits the         properties of an antisolvent), while making use of available         heat.     -   The present embodiment may employ the multi-liquid phase         mixture, which may form before absorption, as a means of cooling         during absorption. For example, the multi-liquid phase mixture         may absorb a portion of the heat resulting from the heat of         absorption through, for example, endothermic phase transition of         the multi-liquid phase mixture into a single liquid phase         solution. may employ cooling for, for example, cooling clouding         or phase change, prior to the absorber. Said benefit may enable         cooling during absorption, including, but not limited to: 1)         without or with less requirement of external cooling during         absorption; 2) reduced delta-T of cooling input (potentially         allowing for a higher input cooling temperature, which may         reduce cooling energy requirements); 3) a combination thereof.

FIG. 2 (A, B) and FIG. 3 (A, B): Summary (FIG. 2A):

An embodiment where one or more desired gases are absorbed in a desired gas lean liquid phase which may comprise at least a portion physical solvent, which may possess, for example, including, but not limited to, higher solubility or capacity or superior absorption properties for one or more desired gases. The absorption of one or more desired gases may result in a desired gas rich liquid, which may be then mixed and dissolved with one or more antisolvent liquid phases, which may result in the formation of a combined single liquid phase. Said antisolvent may comprise one or more liquid phases with lower solubility of one or more desired gases or a liquid phase which may combine with said physical solvent to form a single liquid phase solution with lower solubility of the desired gas or superior properties for desorbing said desired gas or gases, or a combination thereof. Following or during said combining to form two or more liquid phases to form a single liquid phase solution, one or more desired gases may be desorbed from said solution, which may result in a desired gas lean solution and desorbed or captured desired gas. Said resulting desired gas lean single liquid phase solution may be heated (or cooled if said solution exhibits a UCST) to form a multi-liquid phase mixture. Said multi-liquid phase mixture may be separated into two or more separated or partially separated liquid phases using one or more liquid-liquid separation devices. One or more of said separated or partially separated liquid phases may function as the desired gas lean physical absorbent. One or more of said separated liquid phases may function as the antisolvent.

Summary (FIG. 2B):

Similar embodiment to FIG. 2A. The present embodiment may employ desorption to produce captured desorbed gas. Cooling may be employed in the embodiment to facilitate dissolution if, for example, the embodiment exhibits an LCST.

Summary (FIG. 3A):

An embodiment where one or more desired gases may be absorbed in the two or more liquid phases, which may have previously formed from an LCST or UCST phase change. The embodiment employs air stripping of the desired gas or gases.

The two liquid phases shown in FIG. 3A may absorb one or more desired gases in two or more separate absorbers, wherein each absorber may be specific to each of the separated or partially separated liquid phases. This may enable multiple benefits, including, but not limited to, one or more or a combination of the following:

-   -   The liquid phases, including liquid phases with relatively less         desired gas solubility, such as an antisolvent, may be contacted         with the incoming gas and may be enriched with desired gas. This         may ensure the antisolvent, as the liquid phases (including the         antisolvent, if, for example, one or more of the liquid phases         functions as an antisolvent) may be nearly saturated with         desired gas.     -   The absorption units may be cooled below the LCST of the two or         more liquid phases, for example, while the two or more liquid         phases are separate. The liquid phases may be separate and,         thus, may remain separate liquid phases during absorption         rather.     -   May enable selective absorption of one or more gases relative to         one or more other gases in one absorber compared to another         absorber. One or more of said one or more gases, may be, for         example, selectively desorbed or stripped before re-combining         the two or more liquid phases.

Summary (FIG. 3B):

Similar embodiment to FIG. 3A. The present embodiment may employ desorption to produce captured desorbed gas. Cooling may be employed in the embodiment to facilitate dissolution if, for example, the embodiment exhibits an LCST.

Example Inputs and Outputs FIGS. 2A and 3A

Example INPUTS Example OUTPUTS Acid Gas Laden Gas (G-1 and Acid-Gas Lean Gas Stream (G-3 in G-2) 2A, G-4 in 3A) (For example - Air or Other Acid-Gas Lean pure or nearly pure methane) Gas (G-4 in 2A, G-5 in 3A) Acid-Gas Rich Air (G-5 in 2A, Electricity (Gas Compressor, G-6 in 3A) Liquid Pumps, Pretreatment Equipment) Heat Cooling

Example Inputs and Outputs FIGS. 2B and 3B

Example INPUTS Example OUTPUTS Acid Gas Laden Gas (G-1 and Acid-Gas Lean Gas Stream (G-3 in G-2) 2B, G-4 in 3B) (For example - pure Electricity (Gas Compressor, or nearly pure methane) Liquid Pumps, Pretreatment Captured Acid Gas (G-4 in 2B, G-5 Equipment) in 3B) Heat Cooling

Example Step by Step Description:

1. Gas Absorption in Physical Solvent:

-   -   a. FIGS. 2A and 2B: One or more or a combination of gas streams         containing one or more desired gases (G-1) may be pressurized         (Gas Compressor, G-2) and may be contacted with a physical         solvent lean in one or more desired gases (L-1). At least a         portion of one or more desired gases may be absorbed, which may         result in the formation of physical solvent rich in one or more         desired gases (L-2) and/or a gas stream lean in one or more         desired gases (G-3).     -   b. FIGS. 3A and 3B: One or more or a combination of gas streams         containing one or more desired gases (G-1) may be pressurized         (Gas Compressor, G-2) and may be contacted with a physical         solvent lean or antisolvent rich aqueous solution (L-2, Abs #1)         and a physical solvent lean in one or more desired gases (L-1,         Abs #2). At least a portion of the one or more desired gases may         be absorbed, which may result in the formation of physical         solvent rich in one or more desired gases (L-3), antisolvent         rich in one or more desired gases (L-4), and a gas stream lean         in one or more desired gases (G-4).

2. Dissolution of Gas-Rich Physical Solvent into Antisolvent:

-   -   a. FIGS. 2A and 2B: Physical solvent rich in one or more desired         gases (L-2) may be mixed with one or more antisolvent liquid         phases (L-6), which may result in mutual dissolution and may         form a physical solvent-antisolvent combined solution rich in         one or more desired gases (L-3).     -   b. FIGS. 3A and 3B: Physical solvent rich in one or more desired         gases (L-3) may be mixed with an antisolvent solution enriched         with one or more desired gases (L-4), which may result in mutual         dissolution and may form a physical solvent-antisolvent combined         solution rich in one or more desired gases (L-5).

3. Desorption of One or More Gases:

-   -   a. FIG. 2A: Physical solvent-antisolvent combined solution rich         in one or more desired gases (L-3) may be contacted with one or         more stripping gases, such as air or gas lean in one or more         desired gases (G-4) in, for example, one or more gas-liquid         contacting columns (‘Strip/Des’). One or more desired gases may         desorb from said physical solvent-antisolvent combined solution         rich in one or more desired gases into one or more stripping         gases, such as air, which may result in the formation of outlet         air rich in one or more desired gases (G-5) and physical         solvent-antisolvent combined solution lean in one or more         desired gases (L-4).     -   b. FIG. 2B: Physical solvent-antisolvent combined solution rich         in one or more desired gases (L-3) may be depressurized in, for         example, a gas desorption vessel (‘Strip/Des’), which may result         in the desorption of captured one or more desired gases (G-4)         and physical solvent-antisolvent combined solution lean in one         or more desired gases (L-4). The solution may be agitated or         mildly heated (for example: below the cloud-point temperature)         to, for example, facilitate desorption. Another option, may be,         for example: a portion of captured desired gas may be         recirculated and/or sparged into the solution with a pressure         released valve to release a portion of the captured desired gas,         which may enable a portion of the capture desired gas to         function as a stripper or carrier gas and may facilitate desired         gas desorption. Captured desired gas may undergo further         treatment or compression, including, but not limited to, for         example, the removal of a portion of the water vapor.     -   c. FIG. 3A: Physical solvent-antisolvent combined solution rich         in one or more desired gases (L-5) may be contacted with one or         more stripping gases, such as air or gas lean in one or more         desired gases (G-5) in, for example, one or more gas-liquid         contacting columns (‘Strip/Des’). One or more desired gases may         desorb from said physical solvent-antisolvent combined solution         rich in one or more desired gases into one or more stripping         gases, such as air, which may result in the formation of outlet         air rich in one or more desired gases (G-6) and physical         solvent-antisolvent combined solution lean in one or more         desired gases (L-6).     -   d. FIG. 3B: Physical solvent-antisolvent combined solution rich         in one or more desired gases (L-5) may be depressurized in, for         example, a gas desorption vessel (‘Strip/Des’), which may result         in the desorption of captured one or more desired gases (G-5)         and physical solvent-antisolvent combined solution lean in one         or more desired gases (L-6). The solution may be agitated or         mildly heated (for example: below the cloud-point temperature)         to facilitate acid gas desorption. Another option, may be, for         example: a portion of captured desired gas may be recirculated         and/or sparged into the solution with a pressure released valve         to release a portion of the captured desired gas, which may         enable a portion of the capture desired gas to function as a         stripper or carrier gas and may facilitate desired gas         desorption. Captured desired gas may undergo further treatment         or compression, including, but not limited to, for example, the         removal of a portion of the water vapor.

4. Forming a Multiphase Liquid Mixture from Single Liquid Phase Solution:

-   -   a. FIGS. 2A and 2B: Physical solvent-antisolvent combined         solution lean in one or more desired gases (L-4) may be heated         (H-1) to a temperature at or above the cloud-point temperature         or LCST (cooled below a cloud-point temperature in the case a         UCST liquid system is employed), which may result in the         formation of a multi-liquid phase mixture (L-5) comprising one         or more physical solvent liquid phases lean in one or more         desired gases and one or more antisolvent liquid phases lean in         one or more desired gases.     -   b. FIGS. 3A and 3B: Physical solvent-antisolvent combined         solution lean in one or more desired gases (L-6) may be heated         (H-1) to a temperature at or above the cloud-point temperature         or LCST (cooled below a cloud-point temperature in the case a         UCST liquid system is employed), which may result in the         formation of a multi-liquid phase mixture (L-7) comprising one         or more physical solvent liquid phases lean in one or more         desired gases and one or more antisolvent liquid phases lean in         one or more desired gases.

5. Liquid-Liquid Separation and Cooling of Physical Solvent:

-   -   a. FIGS. 2A and 2B: The multi-liquid phase mixture (L-5) may be         separated into one or more physical solvent separated liquids         (L-1) and one or more antisolvent separated liquids (L-6) using,         for example, one or more or a combination of methods for         separating liquid-liquid mixtures (LLS-1). Each stream (for         example: L-1 and L-6) may be cooled before or during or after         the absorption of one or more gases absorption. Said cooling may         be conducted, if desired, after separation of each liquid         stream.     -   b. FIGS. 3A and 3B: The biphasic mixture (L-7) is separated into         a concentrated physical solvent stream (L-1) and a physical         solvent-lean, acid gas lean aqueous solution stream (L-2) using         one or more or a combination of multiphase liquid-liquid         separation methods (LLS-1). Each stream (for example: L-1 and         L-2) may be cooled before or during or after the absorption of         one or more gases absorption. Said cooling may be conducted, if         desired, after separation of each liquid stream.

Example Performance Driving Forces:

-   -   Partial Pressure Equilibrium Swing or Solubility Swing: One of         the underlying principles of the present embodiment may include         the ability of the present embodiment to absorb one or more         desired gases under in a state where the solubility of the         desired gas or gases may be equivalent to or near the solubility         of a high solubility physical absorbent (for example: Selexol or         Rectisol), while the desorption may occur in a state where the         solubility of the desired gas or gases is relatively less than         the state during absorption or similar, equivalent, or less than         the solubility of the desired gas, in a lower gas desired gas         solubility liquid (for example, for acid gases, dilute aqueous         solution, water or salt water solution). Said equilibrium         desired gas solubility shift may occur with the use of         relatively abundant low temperature heat. During absorption, the         primary absorption solution may comprise a rich or nearly pure         physical solvent (which may, for example, comprise physical         solvents known in the art or other physical solvents described         herein), which may exhibit relatively high solubility of one or         more desired gases per unit of physical solvent. To shift the         equilibrium partial pressure to of one or more desired gases         before or during desorption, physical solvent rich in one or         more desired gases may be mixed or dissolved in a solution         exhibiting low solubility of one or more desired gases (for         example: an aqueous salt water solution) or a solution lean in         physical solvent, a combination thereof, or another example         antisolvent. Said dissolving may significantly reduce the         solubility of one or more desired gases in the physical solvent,         resulting in a significant increase in the solubility of one or         more desired gases partial pressure and facilitating the         desorption of one or more desired gases (with, for example, less         required of the heat input generally required to generated         equilibrium shift). After the desorption of one or more desired         gases, the physical solvent may be regenerated from the combined         solution by mildly heating to or above the solution's one or         more LCSTs, if applicable, or cooling below the solution's one         or more UCSTs, if applicable.         -   Higher Solution Capacity:         -   Lower CAPEX, smaller unit size and footprint         -   May possess greater absorption solubility compared to water             and may possess less energy or valuable sources of energy             required from acid gas stripping compared to other physical             solvent processes, such as Selexol.             -   Superior Acidic Gas Desorption Kinetics             -   Partial Pressure Equilibrium Swing without or with                 minimal Heat Input             -   Reduces or Eliminates the Requirement of Heat Input                 during desorption of one or more desired gases     -   Non-Volatile, Non-Toxic, Non-Corrosive Reagents     -   Separating the two or more liquid phases may enable the phases         to be cooled without re-dissolution upon cooling below said         liquid phases LCST. Because the liquid phases are separate, it         may not possible for the liquid phases to dissolve in each other         when they are not in contact with each other.

FIGS. 4 and 5: Summary:

FIGS. 4 and 5 may comprise a similar process to the embodiments shown in FIGS. 2A, 2B, 3A, and 3B. The process may be different in that the phase transition into a multi-liquid phase mixture may be generated by cooling the solution below one or more UCSTs.

Summary (FIG. 4):

An embodiment where the one or more desired gases may be absorbed in one or more desired gas lean physical solvents. The embodiment may employ a liquid system possessing one or more UCSTs, where, for example, a single liquid phase combined solution may be ‘cooled’ below one or more UCSTs, which may result in the formation of a multi-liquid phase mixture. The liquid phases may be at least partially separated using one or more or a combination of liquid-liquid separation devices. In the present embodiment, one or more dissolved gas lean liquid phases, which may possess relatively higher solubility or capacity or superior absorption properties for one or more desired gases, may be transferred to one or more absorption units, where, for example, one or more gases may be absorbed into said one or more liquid phases. Advantageously, the liquid may be relatively ‘cool’ before entering the one or more absorption units as it may be relatively ‘cool’ due to, for example, resulting from being cooled below one or more UCSTs. Said absorption of one or more gases in one or more liquid phases may result in one or more liquid phases rich in one or more dissolved gases. Said one or more liquid phases rich in one or more gases may be mixed with the one or more other liquid phases and/or may be heated to, for example, form a single liquid phase combined solution. Said single liquid phase combined solution may form before, during, or after one or more gas desorption unit (for example: said one or more liquid phases may be heated or mixed or agitated or combination thereof in the desorption unit). Alternatively, the combined single liquid phase solution may form before the desorption unit and then may be transferred to the desorption unit. Advantageously, gas desorption may be facilitated by, including, but not limited to, the dissolution of the of the other phases to form a lower gas solubility combined solution or the heating of said one or more liquid phases or heating of said combined solution or a combination thereof. Because said combined solution may exhibit one or more UCSTs (for example: one or more additional liquid phases or multi-liquid phase solution form upon cooling below one or more UCSTs), gas desorption may be facilitated by both the potential reduced solubility of one or more gases in said combined single liquid phase solution (or, alternatively, in said multi-liquid phase solution) and/or the supply of heat during desorption. Heating and antisolvent solubility reduction may exist simultaneously and may mutually benefit each other. The present embodiment may employ air stripping to, for example, desorb the desired gas or gases. Desorption or flashing of the desired gas or gases to, for example, produce one or more captured gases may also or alternatively be employed.

Summary (FIG. 5):

An embodiment where the one or more gases may be absorbed in the two or more liquid phases, which may be at least partially separated liquid phases. Said two or more liquid phases may have previously formed from one or more phase transitions, for example, which may include, but are not limited to, one or more UCST phase changes in, for example, a liquid system. Said at least partially separated liquid phases may result from the at least partial separation of one or more liquid phases in a multi-liquid phase mixture, which may have resulted from one or more phase transitions. Said one or more liquid phases may absorb one or more gases in one or more separate absorption columns, for example, wherein one or more liquid phases may be separate from one or more other liquid phases during the absorption of one or more gases. The present embodiment may employ air stripping of the desired gas or gases. Also, or alternatively, the embodiment may employ flashing or other form of desorption to form, for example, captured or desorbed gas.

The two or more liquid phases shown in FIG. 5 may absorb gas in two separate absorbers, one absorber may be for each liquid phase. This may enable multiple benefits, which may include, but are not limited to, one or more or a combination of the following:

-   -   One or more liquid phases, which may include liquid phases with         relatively lower solubility of one or more desired gases, may         absorb one or more desired gases. This may prevent dilutive         effects of an antisolvent because, for example, the one or more         liquid phases (which may include one or more antisolvents, if,         for example, one or more of the liquid phases functions as an         antisolvent) may be nearly saturated with desired gas.     -   The absorption units may be cooled below the one or more cloud         point temperatures while the two or more liquid phases may         remain two or more liquid phases. The liquid phases may separate         and, thus, may not dissolve in each other when they are not in         contact. Said separation of liquid phases may be important, for         example, when two or more liquid phases may be desired not to         dissolve in each other under one or more circumstances where,         for example, the temperature of one or more liquid phases may be         at or above one or more UCST and/or at or below one or more         LCSTs.     -   May enable selective absorption of one or more gases relative to         one or more gases in one absorber compared to another absorber.         One or more gases, may be, for example, selectively desorbed or         stripped before re-combining the two or more liquid phases.

One or more at least partially separated liquid phases may be combined and/or heated to form, for example, a combined single liquid phase solution. If, for example, one or more of the liquid phases may be rich in one or more dissolved gases before or during desorption, said combining of said liquid phases may result in greater gas equilibrium partial pressure or lower gas solubility or a solubility equilibrium shift, or combination, as said combined single liquid phase solution may have different solubility properties and/or specifications than, for example, one or more of said separate liquid phases. Advantageously, the combined single liquid phase liquid solution may be heated during desorption, as, for example, said single liquid phase combined solution may continue to be a single liquid phase at elevated temperatures. The one or more benefits of said forming of a combined single liquid phase solution from a multi-liquid phase solution and/or the ability to add heat, potentially simultaneously, or combination thereof, may include, but is not limited to, greater cyclic capacity, desorption rate, absorption rate, lower CAPEX, lower OPEX, higher selectivity, or a combination thereof.

Note:

An alternative embodiment may produce pure CO₂ or other acid gas.

FIG. 6 (A, B): Summary (FIG. 6A):

The present embodiment may employ a ‘basic salt solution’ with physical or physiochemical properties for acid gas absorption or selective absorption of acid gases relative to basic gases or selective absorption of acid gases relative to non-acid gases. Alternatively, the present embodiment may employ an ‘acidic salt solution’ with physical or physiochemical properties for basic gas absorption or selective absorption of basic gases relative to acidic gases or selective absorption of basic gases relative to non-basic gases. Said basic salt solutions may, for example, exhibit a higher solubility of acid gases (for example: CO₂) or other acidic reagents, than, for example, said gases in DI water, however may maintain one or more similar properties or characteristics to physical solvents, which may include, but not limited to, one or more or a combination of the following: not forming a chemical reaction with CO₂ or other acid gas or gases, forming a non-permanent salt with CO₂ or other acid gas or gases with significantly lower reaction energy compared to conventional CO₂ capture absorbents, or a combination thereof. Said acidic salt solutions may, for example, exhibit a higher solubility of basic gases or other basic reagents than, for example, said gases or reagents in DI water, however may maintain one or more similar properties or characteristics to physical solvents, which may include, but not limited to, one or more or a combination of the following: not forming a chemical reaction with basic gases, forming a non-permanent salt with basic gas or gases with significantly lower reaction energy compared to conventional acid scrubbing solutions, or a combination thereof. The present embodiment may employ air stripping to strip one or more absorbed gases. The present embodiment may employ heating to, for example, facilitate desorption of one or more gases. Alternatively, or additionally, the present embodiment may desorb gas to form, for example, one or more captured gases.

Advantages of the present embodiment may include, but are not limited to, one or more or a combination of the following:

-   -   High absorption capacity of one or more acid gases or basic         gases     -   Ultra-low solvent cost     -   Lower pressure operation relative to other physical solvents     -   Resistance to degradation or corrosion or both     -   May not require pretreatment of one or more gases or input gases         streams if desired

Summary (FIG. 6B):

Similar embodiment to FIG. 6A. The present embodiment may employ desorption to produce captured desorbed gas.

Example Inputs and Outputs FIG. 6A

Example INPUTS Example OUTPUTS Acid Gas Laden Gas (G-1 and G-2) Acid-Gas Lean Gas Stream (G-3) Air or Other Acid-Gas Lean Gas Acid-Gas Rich Air (G-5) (G-4) Electricity (Gas Compressor, Liquid Pumps, Pretreatment Equipment) Heat (optional) Cooling (optional)

Example Inputs and Outputs FIG. 6B

Example INPUTS Example OUTPUTS Acid Gas Laden Gas (G-1 and G-2) Acid-Gas Lean Gas Stream (G-3) Electricity (Gas Compressor, (For example - pure or nearly Heat Pump, Liquid Pumps, pure methane) Pretreatment Equipment) Captured Acid Gas (G-4) Heat (optional) Cooling (optional)

Example Step by Step Description:

-   1. Gas Absorption: One or more or a combination of gas streams (G-1)     may be pressurized (Gas Compressor, G-2) and may be contacted with a     basic salt or acidic salt solution lean in one or more desired gases     (L-1). At least a portion of one or desired gases may be absorbed,     which may result in the formation of basic salt or acidic salt     solution rich in one or more gases (L-2) and one or more gas streams     lean in one or more desired gases (G-3). -   2. Gas Desorption:     -   Captured One or More Desired Gases: Basic salt or acidic salt         solution rich in one or more gases (L-2) may be depressurized or         heated or contacted with a condensable stripping gas or a         combination thereof. One or more captured gases (G-4) (may         contain some impurities, which may include, but is not limited         to, water vapor) may be desorbed from said solution, which may         result in the formation of a basic salt or acidic salt solution         lean in one or more desired gases (L-1).     -   Air or Other Carrier Gas Stripping of One or More Desired Gases:         Basic salt or acidic salt solution rich in one or more gases         (L-2) may be depressurized or heated or both and/or may be         contacted with air and/or one or more other gases lean in or         free of one or more desired gases (G-4). Said contacting or         stripping may be conducted in one or more gas-liquid contacting         units (‘ Strip/Des’). One or more desired gases may desorb from         said basic salt or acidic salt solution rich in one or more         gases, which may result in the formation of air containing one         or more desired gases (G-5) and acidic salt or acidic salt         solution lean in one or more gases (L-1).

Example Performance Driving Forces:

-   -   High CO₂ Absorption Capacity     -   Ultra-Low Solvent Cost     -   Drop-in solvent     -   No or relatively minimal degradation of solvent

FIG. 7 (A, B, C): Summary (FIG. 7A):

The present embodiment may employ a ‘basic salt solution’ with physical or physiochemical properties for acid gas absorption or selective absorption of acid gases relative to basic gases or selective absorption of acid gases relative to non-acid gases. Alternatively, or also, the present embodiment may comprise a physical solvent solution.

The present embodiment further comprises one or more ‘acidic reagents’ with concentration dependent on temperature. The solution absorbs acid gas into a basic salt solution lean in acid gas and lean in ‘acidic reagent,’ resulting in a solution rich in acid gas and lean in ‘acidic reagent.’ The solution is then heated to dissolve additional ‘acidic reagent,’ increasing the concentration of the acidic reagent and decreasing the pH and solubility of the acid gas. The increase in ‘acidic reagent’ concentration and the increase in temperature have a noteworthy influence in facilitating an equilibrium or kinetics or combination thereof swing in favor of acid gas desorption.

The embodiment employs a heat exchanger between the solution being heated to dissolve ‘acidic reagent’ and the solution being cooled to precipitate ‘acidic reagent.’ Further heating or cooling may be required to overcome heat exchanger losses, heat exchanger delta-T, or other heat or cooling losses.

Summary (FIG. 7B):

Similar embodiment to the embodiment in FIG. 7A. The present embodiment employs a heat pump (for example: an electric or steam driven heat pump) to provide heat to the ‘acidic reagent’ dissolution unit and provide cooling to the ‘acidic reagent’ precipitation unit. The present embodiment desorbs captured acid gas.

Summary (FIG. 7C):

Similar to the embodiment shown in FIG. 7B. Employs air stripping to strip acid gas or gases.

Inputs and Outputs FIGS. 7A and 7B

Example INPUTS Example OUTPUTS Acid Gas Laden Gas (G-1) Acid-Gas Lean Gas Stream (G-3, Electricity (Gas Compressor, because gas compressor and Heat Pump (7B), Liquid Pumps, compressed gas (G-2) not shown) Pretreatment Equipment) (For example - pure or nearly Heat (optional) (for example: 7B) pure methane) Cooling (optional) (for example: Captured Acid Gas (G-4, because 7B) gas compressor and compressed gas (G-2) not shown)

Inputs and Outputs FIG. 7C

Example INPUTS Example OUTPUTS Acid Gas Laden Gas (G-1 and G-2) Acid-Gas Lean Gas Stream (G-3) Air or Other Acid-Gas Lean Gas (For example - pure or nearly (G-4) pure methane) Electricity (Gas Compressor, Heat Acid Gas Rich Air (G-5) Pump, Liquid Pumps, Pretreatment Equipment) Heat (optional) Cooling (optional)

Note:

The ‘acidic reagent’ is provided as an example ‘CO₂, or other acid gas or gases, Partial Pressure Shifting Reagent.’ Other example applicable reagents or types of reagents are described herein.

Example Step by Step Description:

-   1. Acid Gas Absorption: An acid gas stream (G-1 and G-2 in FIG. 7C)     is contacted with an ‘acidic reagent—lean, acid gas-lean aqueous     basic salt solution’ (L-1), resulting in the absorption of acid gas,     forming an ‘acidic reagent—lean, CO₂-rich aqueous basic salt     solution’ (L-2) and an acid-gas lean gas stream (G-2 in FIGS. 7A and     7B, G-3 in FIG. 7C). -   2. pH Reduction through ‘Acidic Reagent’ Dissolution: The ‘acidic     reagent’—lean, CO₂-rich aqueous ammonia solution (L-2 and L-3) is     transferred to a jacketed mixing vessel (M-1), where it is added to     the pre-existing ‘acidic reagent’ in the vessel and may be heated to     increase the solubility of the ‘acidic reagent’ and facilitate     dissolution. ‘Acidic reagent’ dissolves in the ‘acidic reagent—lean,     CO₂-rich aqueous basic salt solution’, forming an ‘acidic     reagent-rich, CO₂-rich aqueous basic salt solution’ (L-5 and L-7),     which is transferred to ‘step 3’. The increased concentration of     ‘acidic-reagent’ increases the equilibrium partial pressure of CO₂     or other acid gas. -   3. Acid Gas Desorption or Stripping: Acidic reagent-rich, CO₂-rich     aqueous basic salt solution (L-7) enters a stripping or desorption     column.     -   In FIGS. 7A, 7B, and 7C without G-4 (without air stripping),         captured CO₂ desorbs from the solution, forming a high purity         CO₂ (G-4 in 7A and 7B) or other acid gas stream and an ‘acidic         reagent-rich, CO₂-lean aqueous basic salt solution’ (L-8). It         may be saturated with water vapor near desorber or condenser         temperatures.     -   In FIG. 7C, CO₂ is air stripped from the solution (G-4 is input         air), forming a CO₂-rich air stream (G-5) and an ‘acidic         reagent-rich, CO₂-lean aqueous basic salt solution’ (L-8). -   4. Cooling Precipitation of Acidic Reagent: The an ‘acidic     reagent-rich, CO₂-lean aqueous basic salt solution’ (L-10) is cooled     in a controlled precipitation vessel (M-2), precipitating acidic     reagent and forming an ‘acidic reagent—lean, acid gas-lean aqueous     basic salt solution’ (L-12 and L-1).

Example Performance Driving Forces:

-   -   High CO₂ Solution Cyclic Capacity:     -   May not react with some independent weak acids or may react with         independent weak acids with a reversible reaction:     -   Equilibrium swing using reversible reagent     -   Low Solvent Cost     -   No degradation

FIG. 8: Summary FIG. 8:

FIG. 8 may comprise selective gas separation using one or more phase changes. One or more liquid phases may have affinity for one or more gases, which may include, but are not limited to, acid gases or hydrocarbons, while one or more other liquid phases may have affinity for one or more other or different gases, which may include, but are not limited to, acid gases or hydrocarbons. In the embodiment shown in FIG. 8, the one or more gases may be absorbed in a single liquid phase combined solution. The single liquid phase containing both gases may be transformed into a multi-liquid phase mixture, by, for example, change one or more system conditions to, for example, result in one or more phase transitions, UCSTs, or LCSTs. One or more liquid phases may be rich in specific dissolved gases or liquids and lean in other dissolved gases or liquids and one or more liquid phases may be rich in other or different dissolved gases or liquids. Said multi-liquid phase mixture may be rich or lean in opposite dissolved gases or liquids. For example, one liquid phase may be relatively rich in CO₂ and relatively lean in H₂S, while another liquid phase may be relatively rich in H₂S and relatively lean in CO₂. For example, one liquid phase may be relatively rich in CO₂ and relatively lean in H₂S, while another liquid phase may be relatively rich in H₂S and relatively lean in CO₂. For example, one liquid phase may be relatively rich in CO₂, while another liquid phase may be relatively rich in hydrocarbon gases. For example, one liquid phase may be relatively rich in light hydrocarbons or VOCs, while another liquid phase may be relatively rich in heavier hydrocarbons. For example, one liquid phase may be relatively rich in aromatic hydrocarbons, while another liquid phase may be relatively rich in straight-chain hydrocarbons. For example, one liquid phase may be relatively rich polar liquids or dissolved gases, and another liquid phase may be relatively rich in non-polar liquids or dissolved gases. For example, one liquid phase may be relatively rich in methane, while another liquid phase may be relatively rich in ethane. For example, one liquid phase may be relatively rich in natural gas liquids, while another liquid phased may be relatively rich in other gas constituents. For example, one liquid phase may be relatively rich in oxygen, while another liquid phase may be relatively rich in nitrogen.

The concentration of specific dissolved gases in the two or more liquid phases, which may result from one or more phase transitions, may differ between liquid phases. Each liquid phase may have a different concentration of one or more dissolved gases than, for example, the combined solution before phase change. During or after phase change or both, one liquid phase may have a higher affinity for one or more dissolved gases or liquids, while another liquid phase may have a higher affinity for one or more other or different dissolved gases or liquids. Said liquid phases may be separated using a liquid-liquid separation device. Said liquid phases may undergo separate desorption or regeneration processes to remove or capture one or more dissolved gases or liquids. For example, a CO₂-Rich liquid phase may be air stripped and an H₂S-Rich liquid phase may be stripped of H₂S and/or H₂S may be transferred to a Claus Process or may be selectively oxidized in situ to produce, for example, sulfur or a sulfide or sulfur salt, or combination thereof. For example, heavier hydrocarbon rich liquid or petroleum liquids may be stripped and condensed or may be salted out or may be thermally switched or undergo one or more or a combination of methods of remove, recovery or regeneration, or combination thereof. For example, lighter hydrocarbon rich liquid may be stripped and compressed or may be salted out or may be thermally switched or undergo one or more or a combination of methods of removal or recovery of the liquid hydrocarbon. The method of regeneration may be dependent one the one or more dissolved gases or liquids being recovered from one or more specific liquid phases. Said separation of these gases may be more selective and efficient, due to, including, but not limited to, one or more phase transitions resulting in a higher concentration of one or more constituents in one or more liquid phases compared to one or more other constituents.

The present embodiment may be, for example, a technology for separating or concentrating individual components of air. For example, air may be compressed and absorbed into the combined single-phase solution. Said single-phase liquid may be undergo additional changes in system conditions to form or facilitate the formation of a multi-liquid phase mixture. For example, one liquid phase may, for example, have a higher concentration of oxygen than, for example, another liquid phase. For example, one liquid phase may, for example, have a higher concentration of nitrogen than, for example, another liquid phase. For example, one liquid phase may, for example, have a higher concentration of oxygen relative to nitrogen, or vice versa, than, for example, another liquid phase.

One or more dissolved gases in each individual liquid phases may be desorbed in units specific to desorbing said one or more gases in the associated liquid phases. Said desorbed gases may be, for example, higher in relative concentration or partial pressure of oxygen, or for example, higher in relative concentration or partial pressure of nitrogen.

One potential benefit of the above process may be that the gases desorbed may be at similar or greater partial or total pressure than the compressed gas entering the absorber stage. As a result, energetic losses due to pressurization may be minimal, while simultaneously achieving significant partial pressure differences in one or more of the resulting gas phases.

One or more of the resulting desorbed gases may be further concentrated or purified using a membrane, PSA, cryogenic methods, or a combination thereof. One example application for a more concentrated oxygen stream may be in combustion, which may enable, for example, more efficient power generation, higher temperature combustion, and/or the resulting flue gas possessing a have higher concentration of CO₂ or near pure or pure CO₂ (which may enable lower energy consumption and capital cost CO₂ capture).

Example Inputs and Outputs FIG. 8

Example INPUTS Example OUTPUTS Gas #1 and Gas #2 Rich Gas (G-1) Captured Gas #2 (G-6) Gas #1 Lean Air IN (G-4) Gas #1 Rich Air (G-5) Electricity (Gas Compressor, Liquid Pumps, Pretreatment Equipment) Heat Cooling

Example Step by Step Description:

-   1. Gas Absorption: One or more or a combination of gas streams rich     in one or more desired gases (G-1) may be pressurized (Gas     Compressor, G-2) and contacted with a desired gas-lean, single     liquid phase solution (L-1), which may form a gas stream lean in one     or more desired gases (G-3) and a single liquid phase solution rich     in one or more desired gases (L-2).     -   a. Note: In some embodiments, all or almost all gas in G-1 may         absorb, in which case a lean exiting gas may not form. -   2. Phase Transition of Gas Rich Combined Solution into Two or More     Phases: Single liquid phase solution rich in one or more gases (L-2)     may be heated (H-1) to a temperature equal to or above a cloud-point     temperature range for said solution, forming a multi-liquid phase     mixture rich in one or more desired gases (L-3). -   3. Liquid-Liquid Phase Separation: Said multi-liquid phase mixture     rich in one or more desired gases (L-3) may be at least partially     separated into its two or more constituent liquid phases (L-4 and     L-5) using, for example, one or more liquid-liquid separation     devices (LLS-1). -   4. Gas or Liquid Desorption or Regeneration from Each Liquid Phase:     Each at least partially separated liquid phase (L-4, L-5, or more     liquid phases or a combination thereof) may be transferred to one or     more desorption units (Des #1 and Des #2), which may be specifically     designed to desorb or recover one or more dissolved gases or     dissolved liquids or combination thereof. In, for example, Des #2,     dissolved gas #2 rich solution (L-4) may be depressurized or heated     or both, which may result in the desorption of captured desired gas     #2 from solution (G-6) and gas #2 lean solution (L-6). In, for     example, Des #1, dissolved gas #1 rich solution (L-5) may be, for     example, air stripped using, for example, gas #1 lean air (G-4),     which may form gas #1 rich air (G-5) and gas #1 lean solution (L-7). -   5. Gas Lean Liquid-Liquid Phase Mixing and Dissolution: Dissolved     gas #2 lean solution (L-6) and dissolved gas #1 lean solution (L-7)     may be cooled (if, for example, the liquid system exhibits one or     more LCSTs) (CW-1) and mixed, which may result in the dissolution     and the formation of a dissolved gas-lean, single liquid phase     combined solution (L-1).

Example Performance Driving Forces:

-   -   Selective concentrating and separation of dissolved gases due to         multiphasic phase change     -   Higher concentration of one or more dissolved gases relative to         single phase liquid solution     -   Desorption can occur at higher temperatures if desired     -   Desorption can occur under very different conditions using very         different techniques without exposing the other liquid phase or         phases to the same conditions.     -   Higher concentration of one or more dissolved gases relative to         single phase liquid solution equilibrium concentration of         dissolved     -   Capability of stripping one or more dissolved gases under         conditions best suited for stripping one or more dissolved         gases, without exposing the bulk of another dissolved gas to the         same conditions.     -   Superior properties for desorbing one or more dissolved gases in         one or more separate liquid phases relative to the combined         single-phase liquid solution or the concentration of the gases         in the same liquid phase at equilibrium with the input gas         stream     -   Higher concentration of one or more dissolved gases relative to         one or more other dissolved gases in a thermally switched liquid         phase relative to the original combined single-phase liquid         solution     -   Mutual absorption of gases in a common solution, selective         desorption in separate liquid phases.     -   Higher solubility of one or more gases in the combined, single         phase liquid solution than in one or more of the liquid phases         forming from liquid phase change into two or more liquid phases

FIG. 9 (A, B, C) Summary (FIG. 9A):

The present embodiment may pertain to a technology for separating gases.

The present embodiment may absorb one or more gases in a physical solvent exhibiting relatively greater solubility of one or more gases, which may result in a dissolved gas rich physical solvent and a gas stream lean in one or more gases. Said dissolved gas rich physical solvent may be mixed with an antisolvent, which may exhibit relatively low acid gas solubility or have another form of gas solubility changing interaction with said physical solvent. Said mixing may result in the formation of a combined solution. Said combined solution may possess a reduced solubility of one or more gases relative to, for example, said physical solvent, or may exhibit other favorable properties for the desorption of one or more gases. One or more dissolved gases may be desorbed using, for example, including, but not limited to, stripping, air stripping, desorption, depressurization, or a combination thereof, which may result in the formation of a dissolved gas lean combined solution. Said resulting dissolved gas lean combined solution may be regenerated into separated dissolved gas lean physical solvent and antisolvent, using, for example, one or more membrane-based processes. Said dissolved gas lean physical solvent may be, for example, the permeate or concentrate and said antisolvent may be, for example, the permeate or concentrate. For example, said physical solvent may comprise a solution possessing relatively high solubility of one or more gases and/or may comprise one or more reagents with a molecular weight or hydration radius less than the molecular weight cutoff of one or more semi-permeable membranes. For example, said antisolvent may comprise a solution possessing relatively low solubility of one or more gases and/or may comprise one or more reagents with a molecular weight or hydration radius greater than the molecular weight cutoff of one or more semi-permeable membranes. For example, said physical solvent may comprise, including, but not limited to, water or water-organic solvent solution, and said antisolvent, may comprise, including, but not limited to, an aqueous salt, acidic, basic, or combination thereof solution. Alternatively, for example, said physical solvent may comprise a solution possessing relatively high solubility of one or more gases and/or may comprise one or more reagents with a molecular weight or hydration radius greater than the molecular weight cutoff of one or more semi-permeable membranes. Alternatively, for example, the antisolvent may comprise a solution possessing relatively low solubility of one or more gases and/or may comprise one or more reagents with a molecular weight or hydration radius less than the molecular weight cutoff of one or more semi-permeable membranes.

Summary (FIG. 9B):

The present embodiment may pertain to a technology for separating gases.

The present embodiment may absorb one or more gases in a physical solvent exhibiting relatively high solubility for said one or more gases and a separate antisolvent exhibiting relatively low solubility of one or more gases, which may result in a physical solvent rich in one or more dissolved gases, an antisolvent rich in one or more gases, and/or an exiting gas stream lean in one or more gases. Said resulting physical solvent rich in one or more dissolved gases may be mixed with said antisolvent rich in one or more gases (said antisolvent may exhibit relatively low acid gas solubility or have another form of gas solubility changing interaction with said physical solvent), which may result in the formation of a combined solution. Said combined solution may possess a lower solubility of one or more gases relative to, for example, said physical solvent, and/or may exhibit other favorable properties for desorbing one or more gases and/or may be stripped of a portion of one or more gases using, for example, air stripping. Said resulting dissolved gas lean combined solution may be regenerated into separated physical solvent lean in one or more dissolved gases and antisolvent using, for example, one or more membrane-based processes, which may include, but is not limited to, reverse osmosis or nanofiltration. Said acid gas lean physical solvent may comprise a permeate or concentrate and said antisolvent may comprise a permeate or concentrate.

Summary (FIG. 9C):

The present embodiment may pertain to a technology for separating gases.

The present embodiment may absorb one or more gases in a physical solvent exhibiting relatively high solubility for said one or more gases and a separate antisolvent exhibiting relatively low solubility of one or more gases, which may result in a physical solvent rich in one or more dissolved gases, an antisolvent rich in one or more gases, and/or an exiting gas stream lean in one or more gases. Said resulting physical solvent rich in one or more dissolved gases may be mixed with said antisolvent rich in one or more gases (said antisolvent may exhibit relatively low acid gas solubility or have another form of gas solubility changing interaction with said physical solvent), which may result in the formation of a combined solution. Said combined solution may possess a lower solubility of one or more gases relative to, for example, said physical solvent, and/or may exhibit other favorable properties for desorbing one or more gases. One or more gases may be desorbed form the combined solution as captured or separated gas using one or more or a combination of gas desorption methods described herein. Said desorption may result in a combined solution lean in one or more dissolved gases, which may be regenerated into the physical solvent lean in one or more gases and antisolvent lean in one or more gases, using, for example, reverse osmosis, where one or more physical solvents lean in one or more dissolved gases may comprise a permeate or concentrate and one or more antisolvents may comprise a permeate or concentrate.

Example Inputs and Outputs FIGS. 9A and 9B

Example INPUTS Example OUTPUTS Acid Gas Rich Gas (G-1) Acid Gas Lean Gas Acid Gas Lean Air IN Acid Gas Rich Air Electricity (Gas Compressor, Liquid Pumps, Pretreatment Equipment) Heating Cooling

Example Inputs and Outputs FIG. 9C

Example INPUTS Example OUTPUTS Acid Gas Rich Gas (G-1) Captured Acid Gas (G-5) Electricity (Gas Compressor, Liquid Acid Gas Lean Gas (G-4) Pumps, Pretreatment Equipment) Heating Cooling

Example Step by Step Description:

-   1. Gas Absorption:     -   FIG. 9A: One or more or a combination of gas streams rich in one         or more gases (G-1) may be pressurized (Gas Compressor, G-2) and         contacted with one or more physical solvents lean in one or more         dissolved gases (L-1), which may result in a gas stream         relatively lean in one or more gases (G-3) and one or more         physical solvents rich in one or more gases (L-2).     -   FIGS. 9B and 9C: One or more or a combination of gas streams         rich in one or more gases (G-1) may be pressurized (Gas         Compressor, G-2) and contacted with one or more physical         solvents lean in one or more gases (L-1, G-3, Abs #2) and/or one         or more antisolvents lean in one or more gases (L-2, Abs #1),         which may result in a gas stream relatively lean in one or more         gases (G-4), one or more physical solvents relatively rich in         one or more dissolved gases (L-3), or one or more antisolvents         relatively rich in one or more gases (L-4), or a combination         thereof. -   2. Combining Solutions:     -   FIG. 9A: Physical solvent rich in one or more dissolved gases         (L-2) and antisolvent rich in one or more dissolved gases (L-6)         may be combined, which may result in a combined solution (L-3).         Said solvents and/or combined solution may be mixed or heated or         a combination thereof if desired.     -   FIGS. 9B and 9C: Physical solvent rich in one or more dissolved         gases (L-3) and antisolvent rich in one or more dissolved gases         (L-4) may be combined, which may result in a combined solution         (L-5). Said solvents and/or combined solution may be mixed or         heated or a combination thereof if desired. -   3. Gas Desorption:     -   FIG. 9A: Said combined solution rich in one or more dissolved         gases (L-3) may be, for example, stripped, using, for example, a         stripping gas such as air, in one or more desorption units. In         said one or more desorption units, at least a portion of said         one or more dissolved gases may desorb or may desorb into said         stripping gas (G-4). If one or more stripping gases are         employed, said desorbing may result in one or more gas streams         (such as air) rich in one or more desorbed gases (G-5) and one         or more combined solutions lean in one or more dissolved gases         (L-4). Said solution may be depressurized or heated before,         during or after desorption.     -   FIG. 9B: Said combined solution rich in one or more dissolved         gases (L-5) may be, for example, stripped, using, for example, a         stripping gas such as air, in, for example, one or more         desorption units. In said one or more desorption units, at least         a portion of said one or more dissolved gases may desorb or may         desorb into said stripping gas (G-5). Said desorbing may result         in one or more gas streams (such as air) rich in one or more         desorbed gases (G-6) and one or more combined solutions lean in         one or more dissolved gases (L-6). Said solution may be         depressurized or heated before, during or after desorption.     -   FIG. 9C: Said combined solution rich in one or more dissolved         gases (L-5) may enter one or more desorption units. In said one         or more desorption units, at least a portion of one or more         dissolved gases (G-5) may desorb, as, for example, one or more         captured gases, and may result in the formation of a combined         solution lean in one or more dissolved gases (L-6). Before or         during desorption, said one or more combined solutions (L-5) may         be depressurized or heated or a combination thereof. Said one or         more solvents or solutions may be, including, but not limited         to, mixed, depressurized or heated, before, during or after         desorption. To, for example, facilitate desorption, one or more         desorbed gases may be recirculated as, for example, a form of         stripping gas, which may be partially released using, for         example, including, but not limited to a pressure release valve.         Alternatively, or additionally, one or more easily separable         stripping gases, which may be separable using, including, but         not limited to, condensation or gas membrane or combination         thereof, may be employed. -   4. Membrane Based Process or Processes for Regeneration of One or     More Physical Solvents and/or One or More Antisolvents:     -   FIG. 9A: Said combined solution lean in one or more dissolved         gases (L-4) may be pressurized (P-1, L-5) and fed into one or         more membrane-based process units, including, but not limited         to, Reverse Osmosis units. Said membrane-based process units may         form one or more concentrate solutions (which may, for example,         comprise one or more antisolvents or physical solvents) and one         or more permeate solutions (which may, for example, comprise one         or more antisolvents or physical solvents). In FIG. 9A, said         permeate may be shown as a regenerated physical solvent lean in         one or more dissolved gases (L-1) and said concentrate may be         shown as a regenerated antisolvent lean in one or more dissolved         gases (L-6) (for example: the concentrate solution).     -   FIGS. 9B and 9C: Said combined solution lean in one or more         dissolved gases (L-6) may be pressurized (P-1, L-7) and fed into         one or more membrane-based process units, including, but not         limited to, Reverse Osmosis units. Said membrane-based process         units may form one or more concentrate solutions (which may, for         example, comprise one or more antisolvents or physical solvents)         and one or more permeate solutions (which may, for example,         comprise one or more antisolvents or physical solvents). In         FIGS. 9B and 9C, said permeate may be shown as a regenerated         physical solvent lean in one or more dissolved gases (L-1) and         said concentrate may be shown as a regenerated antisolvent lean         in one or more dissolved gases (L-2) (for example: the         concentrate solution).

Example Performance Driving Forces:

-   -   Minimal or practically no antisolvent reagents in the physical         solvent. Reverse osmosis or other membrane-based processes may         exhibit significant selectivity, which may enable a physical         solvent largely without the solubility reducing effects of one         or more antisolvent reagents during, for example, the absorption         of one or more gases.     -   Antisolvent may be mixed with the physical solvent during         desorption gas or acid gas or basic gas solubility swing. The         solubility of one or more dissolved gases may be reduced         compared to, for example, the solubility of one or more gases in         said physical solvent. This, among other benefits, may enable         one or more swings in the equilibrium solubility or partial         pressure or desorption kinetics or combination thereof of one or         more dissolved gases, which may facilitate desorption of one or         more gases or the salting-out of one or more liquids or solids.     -   Relatively low energy consumption of reverse osmosis or         Nano-filtration: Reverse osmosis or nanofiltration         membrane-based processes may generally consume energy at         relatively close to the thermodynamic limits of energy         consumption for aqueous or liquid based separations.     -   High Solubility of one or more dissolved gases in physical         solvent relative to antisolvent     -   Physical solvents may be low cost reagents: Said physical         solvent may comprise, including, but not limited to, water or         other liquids or reagents with hydration radii less than the         molecular weight rejection point or cutoff of one or more         membranes employed in the process or a combination thereof.         Alternatively, said physical solvents may comprise a solution         with one or more reagents greater than the molecular weight         cutoff of one or more membranes.     -   Antisolvents may be low cost reagents: The antisolvents may         comprise, for example, the same solvent as employed in physical         solvents, except with the solubility of one or more gases lower         relative to said antisolvent reagents, including, but not         limited to, acids, acidic salts, bases, basic salts, neutral         salts, one or more reagents with a molecular weight or hydration         radius above the molecular weight rejection point or molecular         weight cutoff of one or more membranes, or a combination         thereof.     -   If desired, selectivity for acid gases or basic gases or one or         more other gases     -   The ability to employ acidic or strongly acidic reagents or         basic or strongly basic reagents in, for example, an         antisolvent: In one or more embodiments, the one or more         solutions may lack basic reagents that may react with acids or         acidic reagents that may react with bases. As a result, the         antisolvent may possess acidity or basicity, if, for example,         said reagents are compatible with one or more membranes or other         process equipment in said one or more embodiments. Higher         acidity reagents may include, but are not limited to, one or         more or a combination of the following: sodium bisulfate,         relatively weak base—relatively strong acid salts, weak acids,         strong acids, organic acids, combinations thereof, or other         reagents described herein. Higher basicity reagents may include,         but are not limited to, one or more or a combination of the         following: potassium carbonate, sodium carbonate, sodium         hydroxide, ammonia, amine, ammonium carbonate, strong base-weak         acid, strong base, weak base, or organic bases.     -   Two or more different absorbers or absorption units for         absorbing one or more gases in physical solvent and/or         antisolvent: May enable physical solvent and/or antisolvent to         be rich in in one or more dissolved gases before mixing,         potentially maximizing acid gas desorption and partial pressure         swing.     -   Resistance to degradation     -   Compatibility with potential gas impurities

-   Note: In an alternative version of the present embodiment, one or     more gases may be dissolved in a combined single liquid phase     solution, which may form a combined single liquid phase solution     rich in one or more dissolved gases. Said combined solution may be     separated into two or more liquid solutions using one or more     membrane-based processes. One or more of said two or more liquid     solutions may be rich in or selective for one or more gases.     Alternatively, or also, said two or more liquid solutions may be     rich in or selective for one or more different gases. In the present     embodiment, one or more of said liquid phases may comprise one or     more reagents with a molecular weight cutoff or hydration radius     greater than the molecular weight cutoff of one or more membranes or     sufficiently large to be at least partially rejected by said one or     more membranes. Said one or more reagents may increase or decrease     the solubility of one or more dissolved gases relative to, for     example, one or more of the other liquid phases. The present     embodiment may be similar to the example embodiments in FIG. 8,     except may employ one or more membrane-based processes to form two     or more liquid phases or separate liquid solutions from a single     liquid phase solution, rather than, or in addition to, a liquid     phase transition or UCST or LCST.

Summary Active Cloud Point Adjustment:

Embodiments described herein may employ systems and methods for actively adjusting the cloud point or LCST or UCST or a combination thereof. Active cloud point adjustment may comprise changing the compositions of one or more or a combination of liquid phases to increase or decrease or maintain one or more LCSTs or UCSTs or combination thereof. Active cloud point adjustment may involve removing a portion of one or more liquid system reagents, or re-introducing additional one or more liquid system reagents, or adding one or more external reagents to a liquid system, or removing one or more external reagents from a liquid system. Active cloud point adjustment may involve changing one or more system conditions to adjust cloud point. Active adjustments of cloud point may be desirably reversible. Active cloud point adjustment may be in response to, for example, changes in one or more system conditions or compositions or economic factors. Said changes may include, but are not limited to, one or more or a combination of the following: changes in the temperature of one or more available heat sources, changes in the temperature of one or more available cooling sources, changes in outside temperature, changes in pressure, changes in composition of one or more input gas streams, the dissolved concentration of one or more gases affecting cloud point temperature, changes in the value of inputs or outputs, the presence or lack of presence of one or more reagents, degradation, impurities, or a combination thereof.

Example Embodiment for Active Cloud Point Adjustment in an LCST Liquid System:

An embodiment for active adjustment of cloud point may involve reversibly adjusting the concentration of one or more reagents which may have influence on the one or more LCSTs, UCSTs, phase transitions, the composition of or one or more liquid phases, the relative mass of one or more liquid phases, the relative volume of one or more liquid phases, or a combination thereof. For example, a LCST liquid system may comprise, including, but not limited to, one or more or a combination of the following: 1) one or more polymers, 2) water, 3) one or more reagents insoluble or exhibiting low solubility in said one or more polymers without the presence of water, or 4) one or more reagents soluble in said polymer and/or water. Said example LCST liquid system and/or other example liquid systems may employ one or more or a combination of the following example systems & methods for adjusting LCST. The present embodiment may employ a membrane-based process and/or the addition of a ‘permeate’ liquid or ‘permeate equivalent liquid’ to adjust one or more or a combination cloud points.

-   -   Decreasing LCST:     -   The present example embodiment may involve first forming a         multi-liquid phase solution, which may involve a phase         transition before or during the present example embodiment. One         or more of said liquid phases in said multi-liquid phase         solution may comprise an aqueous solution lean in one or more         polymers. The present embodiment may employ one or more         multi-liquid phase liquid-liquid separation devices, which may         separate said liquid phase aqueous solution lean in one or more         polymers from one or more other liquid phases. Said separated         liquid phase aqueous solution lean in one or more polymers may         comprise, for example, water, one or more salts (or other         reagents which facilitate reduction of LCST cloud point), and/or         residuals of non-rich reagents (for example: polymer). Said         solution may be concentrated using, for example, one or more         membrane-based process, such as reverse osmosis and         nanofiltration.     -   In one version of the present embodiment, the liquid phase         aqueous solution lean in one or more polymers may comprise a         feed solution to a reverse osmosis system, wherein said salt and         residual polymer may be concentrated, forming, for example, a         concentrate. A portion of water and other reagents not rejected         or fully rejected by the one or more membranes may pass through         said one or more membranes, forming, for example, a permeate         liquid or permeate liquid mixture (liquid mixture may form, for         example, if one more reagents are insoluble or exhibit limited         solubility without or with less presence of one or more reagents         rejected by said one or more membranes). A liquid system         containing said concentrate solution may possess a lower LCST         than the LCST of the liquid system before treatment with one or         more membranes. Relatively higher concentration of, for example,         salt, may decrease the LCST of liquid system. Said permeate,         may, for example, be stored. Said permeate liquid may be later         re-introduced into a liquid system. For example, said permeate         liquid may be added to said liquid system to, for example,         increase the one or more LCSTs.     -   In another version of the present embodiment said liquid phase         aqueous solution lean in one or more polymers may first undergo         separation of one or more residual polymers from a portion of         the remaining solution. Said first separation may involve         concentrating one or more of said residual polymers using one or         more semi-permeable membranes. It may be desirable for said         permeable membranes to reject one or more of said polymers,         while, for example, allowing one or more other reagents to pass         through the membrane. Said semi-permeable membranes may         comprise, including, but not limited to, nanofiltration or         ultrafiltration. Said concentrating may resulting in a polymer         rich concentrate solution or mixture and a polymer-lean or         polymer-free permeate. Said polymer concentrate may be         re-introduced into the liquid system or stored for later use or         re-introduction to the liquid system or combination thereof.         Said polymer-lean or polymer-free permeate may comprise,         including, but not limited to, one or more or a combination of         the following: water, or salts, or other reagents which         influence phase transition, or combination thereof. Said         polymer-lean or polymer-free permeate may be concentrated in a         second separation using one or more semi-permeable membranes,         for example, reverse osmosis, which may be able to concentrate         or reject one or more reagents unrejected or minimally rejected         by said first separation. Said second separation may form a         concentrate solution more concentrated in salts or other         reagents which may influence phase transition or combination         thereof and a permeate solution lean in said one or more         reagents. Said concentrate may be re-introduced into the liquid         system, which may decrease said liquid system's phase transition         temperature (such as a LCST) or multi-liquid phase composition         or multi-liquid phase distribution, other adjustments to said         liquid systems cloud point or phase transition, or a combination         thereof. Said permeate liquid may be later introduced into a         liquid system. For example, said permeate liquid may be added or         later added to said liquid system to, for example, increase the         one or more LCSTs.     -   In another version of the present embodiment, a single liquid         phase combined solution may be concentrated using one or more         membranes.         -   A) For example, said single liquid phase may be first             concentrated using one or more membrane which rejects one or             more larger molecular weight reagents, such as residual             polymers, while, for example, allowing smaller molecular             weight reagents, such as salts or low molecular weight             organics or water, to pass through said membranes. Examples             of said membranes, may include, but are not limited to,             nanofiltration or ultra-filtration membranes or other             semi-permeable membrane systems & methods described in             herein. Said concentrating may form a concentrate solution             rich in said one or more larger molecular weight reagents,             and a permeate stream lean or free of said larger molecular             weight reagents. Said concentrate solution may be stored or             introduced into the liquid system. Said permeate may be             returned to the liquid system or may undergo one or more             further steps, for example, step B).         -   B) Said permeate may be concentrated in a second             concentrating step using one or more semi-permeable             membranes, for example, reverse osmosis, which may be able             to concentrate or reject one or more reagents unrejected or             minimally rejected by said first concentrating step. Said             second concentrating step may form a concentrate solution             more concentrated in salts or other reagents which may             influence phase transition or combination thereof and a             permeate solution lean in said one or more reagents. Said             concentrate may be re-introduced into the liquid system,             which may decrease said liquid system's phase transition             temperature (such as an LCST) or multi-liquid phase             composition or multi-liquid phase distribution, other             adjustments to said liquid system's cloud point or phase             transition, or a combination thereof. Said permeate liquid             may be later introduced into a liquid system. For example,             said permeate liquid may be added or later added to said             liquid system to, for example, increase the one or more             LCSTs.         -   Alternatively, said single liquid phase combined solution             may be first concentrated using reverse osmosis. Said             concentrating may reject polymer or salts or one or more             other reagents which may influence phase transition or a             combination thereof. Said concentrating may result in             concentrate solution or multi-liquid phase mixture more             concentrated in polymer and salts or one or more other             reagents and a permeate solution lean in one or more or             nearly all or all said reagents. Said concentrate solution             or multi-liquid phase mixture may exhibit a lower LCST             relative to the input single liquid phase combined solution.             Said concentrate solution may be introduced to the liquid             system or may comprise a component of the liquid system.             Said permeate liquid may be later introduced into a liquid             system. For example, said permeate liquid may be added or             later added to said liquid system to, for example, increase             the one or more LCSTs.     -   Increasing LCST:     -   LCST of a liquid system may be increased, for example, by adding         permeate liquid or permeate equivalent liquid to said liquid         system. Said permeate liquid may desirably be lean or         essentially free of salts or other reagents which may decrease         LCST when in one or more liquid systems. Said addition of         permeate liquid or permeate equivalent liquid may, for example,         dilute or reduce the concentration of one or more salts or other         reagents which may influence LCST, which may result in an         increase in LCST temperature.

Example Embodiment for Active Cloud Point Adjustment in UCST System:

An embodiment for active adjustment of cloud point may involve reversibly adjusting the concentration of one or more reagents which may have influence on the one or more LCSTs, UCSTs, phase transitions, the composition of or one or more liquid phases, the relative mass of one or more liquid phases, the relative volume of one or more liquid phases, or a combination thereof. For example, a UCST liquid system may comprise, including, but not limited to, one or more or a combination of the following: 1) one or more polymers, 2) water, 3) one or more reagents insoluble or exhibiting low solubility in said water without the presence of polymer and/or one or more other reagents, or 4) one or more reagents soluble in said polymer and/or water. Said example UCST liquid system and/or other example liquid systems may employ one or more or a combination of the following example systems & methods for adjusting UCST. The present embodiment may employ a membrane-based process and/or the addition of a ‘permeate’ liquid or ‘permeate equivalent liquid’ to adjust one or more or a combination cloud points.

-   -   Decreasing UCST: The present example embodiment may involve         first forming a multi-liquid phase solution, which may involve a         phase transition before or during the present example         embodiment. One or more of said liquid phases in said         multi-liquid phase solution may comprise a solution containing         one or more polymers. In some UCST liquid systems described         herein, one or more polymers may function as a necessary reagent         (for example: polypropylene glycols or polyethylene glycols) to         ensure another one or more reagents (for example: propylene         carbonate) are soluble in yet another reagent (for example:         water) at or below one or more UCSTs. Furthermore, in one or         more embodiments described herein, the concentration of said         polymer relative to said one or more other reagents may         influence the UCST of the liquid system. For example, in some         liquid systems, an increase in concentration of, for example,         PPG 425, relative to propylene carbonate and/or water, may         decrease said UCST. One or more of said liquid phases comprising         one or more polymers may be separated, in part or in whole, or         may remain a multi-liquid phase mixture. Said one or more liquid         phases comprising a solution containing one or more polymers may         be concentrated using one or more semi-permeable membranes, for         example, which may include, but are not limited to, reverse         osmosis (RO), nanofiltration (NF), or ultrafiltration (UF). To         decrease cloud point temperature, it may be desirable for said         one or more semipermeable membranes to reject one or more         polymers, while, for example, allowing other reagents to pass         through said membrane. By concentrating one or more polymers,         while allowing other reagents to pass through said         semi-permeable membrane, salts and other reagents which may         increase UCST, if any, may remain at similar or the same         concentration in solution. Said concentrating may result in a         concentrate solution, which may possess a greater concentration         of one or more polymers, and/or a permeate solution, which may         comprise a liquid or multi-liquid phase mixture lean or free of         one or more polymers. Said concentrate may be re-introduced into         the liquid system, which may decrease said liquid system's phase         transition temperature (such as an UCST) or multi-liquid phase         composition or multi-liquid phase distribution, other         adjustments to said liquid system's cloud point or phase         transition, or a combination thereof. Said permeate liquid may         be later introduced into a liquid system. For example, said         permeate liquid may be added or later added to said liquid         system to, for example, increase the one or more UCSTs. In         another version of the present embodiment, a single liquid phase         combined solution may be a feed solution concentrated using one         or more semi-permeable membranes. For example, one or more         polymers in said single liquid phase combined solution may be         concentrated. Said concentrating may result in a concentrate         solution with a greater concentration of one or more polymers         relative to the said feed solution and a permeate solution lean         or substantially free of said one or more polymers. In the         substantial absence of one or more polymers, one or more of said         reagents in said permeate may be mutually insoluble or exhibit         limited solubility in each other, which may result in, for         example, the resulting permeate comprising a multi-liquid phase         mixture. Said concentrate solution may exhibit a lower UCST due         to, for example, greater polymer concentration. Said permeate         liquid may be later introduced into a liquid system. For         example, said permeate liquid may be added or later added to         said liquid system to, for example, increase the one or more         UCSTs.     -   Increasing UCST:     -   The UCST of a liquid system may be increased, for example, by         adding permeate liquid or permeate equivalent liquid to said         liquid system. Said permeate liquid may dilute or reduce the         concentration of one or more polymers, which may enable an         increased UCST.     -   Alternatively, or additionally, UCST may be increased using, for         example, a membrane separation process. For example, if a UCST         liquid system may contain salts or one or more other reagents         which may increase UCST, one or more of said reagents may be         concentrated. In one version of the present embodiment, said         concentrating may occur in by concentrating a solution lean or         free of one or more polymers (for example: the permeate from a         polymer concentrating or separation step using, for example,         nanofiltration or ultrafiltration). Said concentrating a         solution lean or free of one or more polymers may be desirable         as it may prevent the substantial simultaneous concentrating of         one or more polymers.

Summary FIG. 10 (A-C):

FIG. 10A-C may show an example embodiment employing example systems and methods for active cloud point adjustment. The present embodiment may employ said active cloud point adjustment to, for example, actively adjust one or more UCSTs in the embodiment's liquid system. The present embodiment for cloud point adjustment may actively adjust said solution's cloud point by, including, but not limited to, one or more or a combination of the following: changing UCST through one or more nanofiltration concentrating steps or changing UCST through the addition of permeate or permeate equivalent or changing UCST through one or more reverse osmosis concentrating steps or maintaining composition or cloud point by, for example, by-passing composition adjustment steps.

Step-by-Step Description:

The present embodiment may start with, for example, a liquid in a liquid system with one or more cloud points. The liquid may have a UCST (or may have a LCST) and may comprise a single liquid phase combined solution or a multi-liquid phase mixture solution. FIG. 10A may show a single liquid phase combined solution (L-4) as an example. Said solution may be transferred to one of two or three pathways depending on, for example, if one or more cloud points of said solution or liquid system may need to be increased, decreased, or remained constant. If, for example, one or more cloud points of said liquid system may need to be decreased, it may be desirable for one or more of the reagents which may decrease cloud point to be concentrated, using, for example, nanofiltration. Said concentrating with nanofiltration may involve pressurizing the solution (L-6) using one or more pumps (P-1), which may form a pressurized feed solution (L-8) to be concentrated in one or more nanofiltration units (NF). Said feed solution may be fed into one or more nanofiltration units, which may result in a concentrate stream (L-10) and a permeate stream (L-9). Said concentrate stream (L-10) may possess a greater concentration of, for example, one or more reagents which decrease cloud point, which may include, but are not limited to, one or more reagents which may be rejected by said one or more nanofiltration units. Said concentrate stream may be returned to said liquid system or comprise the liquid system or, in other words, may be returned to, for example, the gas separation process. Said concentrate stream may possess a lower UCST than said feed solution. Said permeate solution may be transferred to one or more liquid storage vessels (‘Permeate Storage’). Said permeate may be re-introduced into the liquid system, for example, upon the need for active increase in UCST. If, for example, one or more cloud points of said liquid system may need to be increased, it may be desirable for said solution to be mixed with permeate or permeate equivalent liquid (L-11, ‘Merge #1). Said mixing with permeate or permeate equivalent may dilute or reduced the concentration of one or more reagents which may decrease UCST, which may result in an increase in one or more UCSTs. Said solution mixed with permeate may be returned to said liquid system or comprise the liquid system or, in other words, may be returned to, for example, the gas separation process. If, for example, one or more cloud points of said liquid system may need to be unadjusted, said solution may be transferred to the next stage of the gas separation process without, for example, adjusting its composition. Alternatively, or additionally, one or more UCSTs may be adjusted by one or more membranes-based processes (for example: reverse osmosis), which may be conducted by concentrating one or more reagents which may increase cloud point temperature with increased concentration in the liquid system. For example, the present embodiment may involve first forming a multi-liquid phase mixture by, for example, cooling a liquid system to at or below one or more UCSTs. Then, the present embodiment may involve at least partially separating said multi-liquid phase mixture into two or more of its constituent liquid phases. One or more of said constituent liquid phases may be lean in one or more reagents which decrease UCST at greater concentrations and may possess sufficiently large molecular weight or hydration radius to be at least partially rejected by a reverse osmosis membrane. Said one or more ‘lean’ liquid phases may contain one or more reagents which increase UCST with increased concentration and may possess sufficiently large molecular weight or hydration radius to be at least partially rejected by a reverse osmosis membrane. Said one or more ‘lean’ liquid phases may be a feed solution in one or more membrane based concentrating steps. Said one or more membrane based concentrating steps may include one or more concentrating steps to increase the concentration of one or more reagents which increase UCST with increased concentration. Said one or more membrane based concentrating steps may result in the formation of a concentrate solution and a permeate solution. Said concentrate solution may possess a greater concentration of one or more reagents which increase UCST with increased or greater concentration of said one or more reagents reagent. Said concentrate solution may be introduced into the liquid system, which may involve mixing one or more liquid phases in the liquid system or re-formation of a UCST liquid system. Said concentrate may increase one or more of the UCSTs of the liquid system relative to the liquid system before said concentrating. Said permeate solution may comprise a solution lean or free of one or more reagents which appreciably influence the UCST of the liquid system. Said permeate solution may be stored. Said permeate solution may be later introduced or added to the liquid system to, for example, decrease one or more UCSTs. FIG. 10A Cloud Point Adjustment Description: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more UCST phase transitions. FIG. 10A may show the present embodiment undergoing active liquid system cloud point adjustment to, for example, decrease one or more UCSTs. FIG. 10B Cloud Point Adjustment Description: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more UCST phase transitions. FIG. 10B may show the present embodiment undergoing active liquid system cloud point adjustment to, for example, increase one or more UCSTs. FIG. 10C Description: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more UCST phase transitions. FIG. 10C may show the present embodiment maintain one or more UCSTs, or composition of liquid phases, or bypassing of permeate addition or membrane-based concentrating, or combination thereof.

Summary FIG. 11:

FIG. 11A-C may show an example embodiment employing example systems and methods for active cloud point adjustment. The present embodiment may employ said active cloud point adjustment to, for example, actively adjust one or more LCSTs in the embodiment's liquid system. The present embodiment for cloud point adjustment may actively adjust said solution's cloud point by, including, but not limited to, one or more or a combination of the following: changing LCST through one or more reverse osmosis concentrating steps or changing LCST through the addition of permeate or permeate equivalent or changing LCST through one or more nanofiltration concentrating steps or maintaining composition or cloud point by, for example, by-passing composition adjustment steps.

Step-by-Step Description:

The present embodiment may start with, for example, a liquid in a liquid system with one or more cloud points. The liquid may have a LCST (or may have a UCST) and may comprise a single liquid phase combined solution or a multi-liquid phase mixture solution. Said solution may be transferred to one of two or three pathways depending on, for example, if one or more cloud points of said solution or liquid system may need to be increased, decreased, or remained constant. If, for example, a liquid system requires a decrease in one or more LCSTs, one or more LCSTs may be adjusted by membrane-based concentrating (for example: Reverse Osmosis) of one or more reagents which may decrease cloud point temperature with increased concentration in the liquid system. For example, the present embodiment may involve first forming a multi-liquid phase mixture by, for example, heating a liquid system to at or above one or more LCSTs. Then, the present embodiment may involve at least partially separating said multi-liquid phase mixture into two or more of its constituent liquid phases. One or more of said constituent liquid phases may contain a relatively greater concentration of one or more reagents which decrease LCST with increased concentration, one or more of said reagents which may possess sufficiently large molecular weight or hydration radius to be at least partially rejected by a reverse osmosis membrane. Said one or more liquid phases rich in one or more reagents which decrease LCST with increased concentrations may be one or more feed solutions in one or more membrane based concentrating steps. Said one or more membrane based concentrating steps may include one or more concentrating steps to increase the concentration of one or more reagents which decrease LCST with increased concentration. Said one or more membrane based concentrating steps may result in the formation of a concentrate solution and a permeate solution. Said concentrate solution may possess a greater concentration of one or more reagents which decrease LCST with increased or greater concentration in an example liquid system. Said concentrate solution may be introduced into one or more liquid systems, which may involve mixing one or more liquid phases in a liquid system or re-formation of a LCST liquid system. Said concentrate may increase one or more of the LCSTs of the liquid system relative to the liquid system before said concentrating. Said permeate solution may comprise a solution lean or free of one or more reagents which appreciably influence the LCST of a liquid system. Said permeate solution may be stored. Said permeate solution may be later introduced or added to a liquid system to, for example, increase one or more LCSTs. If, for example, a liquid system requires an increase in one or more LCSTs, one or more LCSTs may be adjusted by, for example, adding permeate or permeate equivalent solution to said liquid system. The reduced concentration of one or more reagents which decrease LCST with increasing concentration may result in an increase in the one or more LCSTs of said liquid system. If, for example, one or more cloud points of said liquid system may need to be unadjusted, said solution may be transferred to the next stage of the gas separation process without, for example, adjusting its composition. FIG. 11A Cloud Point Adjustment Description: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more LCST phase transitions. FIG. 11A may show the present embodiment undergoing active liquid system cloud point adjustment to, for example, decrease one or more LCSTs. FIG. 11B Cloud Point Adjustment Description: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more LCST phase transitions. FIG. 11B may show the present embodiment undergoing active liquid system cloud point adjustment to, for example, increase one or more LCSTs. FIG. 11C Description: The present embodiment may comprise systems and methods for gas separation. The present embodiment may employ one or more LCST phase transitions. FIG. 11C may show the present embodiment maintain one or more LCSTs, or composition of liquid phases, or bypassing of permeate addition or membrane-based concentrating, or combination thereof.

Exemplary Embodiments For Example: Gas Separation—Cloud Point without Liquid-Liquid Separation

-   -   Process for separating gases comprising: [Physical absorption         gas separation with antisolvent to facilitate gas desorption]     -   Process for separating acid gases comprising: [Water or an         aqueous solution rich phase exhibits lower acid gas solubility         and organic-rich phase exhibits greater acid gas solubility]     -   Process for separating gases comprising: [Water or an aqueous         solution rich phase exhibits lower acid gas solubility and         organic-rich phase exhibits greater acid gas solubility]     -   Process for separating acid gases comprising: [Water or an         aqueous solution functions as an antisolvent to facilitate acid         gas desorption while organic-rich thermally reversible phase         functions as the physical absorbent]     -   Process for separating acid gases comprising: [recovery of the         enthalpy of absorption during absorption in physical absorbent         through an endothermic phase change]     -   Process for separating acid gases comprising: [Absorbing in a         medium with more liquid phases than the medium for desorption]     -   Process for separating acid gases comprising: [Absorbing in a         two or more-phase liquid, desorbing in a single-phase liquid]     -   Process for separating acid gases comprising: [Absorbing in a         single-phase liquid, desorbing in a two-phase liquid]     -   Process for separating acid gases comprising: [acid gases are         more soluble in two phases solutions than one phase solution]         -   Absorbing acid gases in a     -   Process for separating gases comprising: [Absorbing in X liquid         phases, desorbing with X+n liquid phases]     -   Process for separating gases comprising: [Absorbing in X+n         liquid phases, desorbing with X liquid phases]

Exemplary Sub-Embodiments (Cloud Point with Liquid-Liquid Separation)

-   -   Wherein one liquid phase is selective for one or more gases and         the other liquid phase is selective for one or more gases     -   Wherein one liquid phase is selective for one or more gases and         the other liquid phase is selective for one or more different         gases     -   Wherein the antisolvent reduces acid gas solubility by one or         more or a combination of the following: forming a combined         solution with a lower acid gas solubility than the two or more         separate phases, providing heat before or during desorption due         to the enthalpy of dissolution, providing entropy before or         during desorption due to the entropy of dissolution     -   Wherein the antisolvent and physical solvent phases are         regenerable using thermally switchable solubility     -   Wherein the organic rich phase is rich in organic solvent,         organic polymer, or a combination thereof     -   Wherein the organic rich phase is non-volatile     -   Wherein the ‘high acid gas solubility phase’ is non-volatile     -   Wherein the ‘high acid gas solubility phase’ is rich in organic         solvent, organic polymer, or a combination thereof     -   Wherein the ‘low acid gas solubility phase’ is rich in water,         one or more ionic compounds, one or more relatively lower acid         gas solubility reagents, or a combination thereof     -   Wherein the two or more liquid phases are reversibly regenerated         from a solution or mixture with less phases     -   Wherein the two or more liquid phases are reversibly regenerated         from a single liquid phase solution     -   Wherein the two or more liquid phases are regenerated using one         or more or a combination of the following: thermally switchable         solubility, cloud point, membrane, changes in pressure, changes         in solubility, changes in system conditions, reversible changes         in system conditions     -   Organic reagent compositions     -   Wherein said phase change comprises forming a two or more-phase         liquid solution from a single-phase liquid solution     -   Wherein said phase change comprises forming a single-phase         liquid solution from a two or more-phase liquid solution     -   Wherein said phase change comprises forming a multiphase liquid         solution with more liquid phases than the input solution     -   Wherein said phase change comprises forming a liquid solution         with less liquid phases than the input multiphase liquid         solution     -   Wherein the phases are separated using a liquid-liquid         separation device     -   Wherein the phases remain as a mixture throughout the integrated         process     -   Wherein the liquid-liquid cloud point occurs from heating above         one or more cloud-point temperature ranges     -   Wherein the liquid-liquid cloud point occurs from cooling below         one or more cloud-point temperature ranges     -   Water or an aqueous solution rich phase and organic-rich phase         exhibit similar acid gas solubility     -   Water or an aqueous solution rich phase and organic-rich phase         exhibit different acid gas solubility     -   Water or an aqueous solution rich phase and organic-rich phase         undergo a positive entropy phase change and reversing said phase         change constitutes and negative entropy phase change     -   Acid gas separation     -   Hydrocarbon separation     -   (For Example: Employing Membrane Concentrating, Acidic Reagent         Solution, Salt Solution, Freshwater Absorption Solution,         Physical Solvent Absorption Solution, Antisolvent Solution or         Combination Thereof)

Exemplary Embodiments

-   -   Process for separating gases comprising:         -   An absorption solution comprising separated physical solvent         -   Wherein gas rich physical solvent is mixed with an             antisolvent solution         -   Wherein gas is desorbed or stripped from said mixed solution     -   Process for separating gases comprising:         -   An absorption solution comprising separated physical solvent         -   Wherein gas rich physical solvent is mixed with an             antisolvent solution         -   Wherein acid gas is desorbed or stripped from said mixed             solution

Exemplary Sub-Embodiments

-   -   Wherein said mixed solution is regenerated into physical solvent         and antisolvent using a membrane-based separation device     -   Wherein the antisolvent is also enriched with acid gas     -   Wherein the antisolvent is also enriched with acid gas during         absorption     -   Wherein the antisolvent is also enriched with acid gas in a         separate absorption unit     -   Wherein said antisolvent facilitates the desorption of said         gases from solution     -   Wherein said mixed solution is regenerated into physical solvent         and antisolvent using reverse osmosis, forward osmosis, membrane         distillation, or a combination thereof     -   Wherein the antisolvent contains one or more reagents with a         molecular weight greater than the molecular weight cutoff of the         membrane or membranes employed to separate the antisolvent         reagents from the physical solvent     -   Wherein the antisolvent contains one or more reagents capable of         being rejected by a membrane or membranes employed to separate         the antisolvent reagents from the physical solvent     -   Wherein the antisolvent comprises one or more or a combination         of the following: acid, organic acid, inorganic acid, acid with         a hydration radius greater than 80 da, organic acid with a         hydration radius greater than 80da, ionic compound, acidic ionic         compound, weak base—strong acid, cation-hydrogen or         dihydrogen-anion salt, alkali hydrogen sulfate salt,         ammonium—strong acid salt, citric acid, water, organic solvent     -   Wherein the antisolvent comprises an acid, an acidic salt,         acidic polymer, or a salt or a combination thereof in addition         to the same liquid components as the physical solvent     -   Wherein the solubility of one or more gases in the combined         solution is less than the solubility of one or more gases in the         individual liquid phases     -   Wherein the solubility of one or more gases in the physical         solvent is greater than the solubility of one or more gases in         the antisolvent     -   Wherein said physical solvent comprises a liquid with a molar         mass below the molecular weight cutoff of the membrane or         membranes employed to separate the antisolvent reagents from the         physical solvent     -   Wherein said physical solvent comprises one or more or a         combination of the following: liquid with a molecular weight         below the molecular weight cutoff of one or more membranes         employed herein, water, organic solvent, non-volatile organic         solvent, propylene glycol, ethylene glycol, propylene carbonate,         glycerol, urea     -   Wherein said physical solvent may contain antisolvent,         including, but not limited to, as an impurity     -   Wherein said gases comprise one or more or a combination of the         following: acid gases, basic gases, hydrocarbons, inert gases,         air     -   Wherein said antisolvent functions to facilitate gas desorption     -   In the absence of the formation of a solid precipitate     -   In the absence of the formation and removal of a solid         precipitate     -   (For Example: Selective Gas Separation using Thermally Switching         Phase Change with Liquid-Liquid Separation)

Exemplary Embodiments

-   -   Process for separating gases comprising:         -   Absorption of two or more gases in a single liquid phase to             form gas-rich liquid phase         -   Heating or cooling said gas-rich liquid phase to form two or             more liquid phases         -   Wherein at least one of said two or more liquid phases             comprises one or more or a combination of the following:             -   a) higher concentration of one or more gases relative to                 one or more gases compared to the original single liquid                 phase solution             -   b) superior properties for desorption of one or more                 gases compared to said single liquid phase solution     -   Process for separating gases comprising [absorption of one or         more gases in a single physical solvent liquid phase to form         gas-rich liquid phase, heat or cooling said gas enriched liquid         phase to form two or more liquid phases, desorbing said gases         from at least one of said two or more liquid phases]:     -   Process for separating gases comprising: [Absorbing in X liquid         phases, desorbing with X+n liquid phases]     -   Process for separating gases comprising: [Absorbing in X+n         liquid phases, desorbing with X liquid phases]

Exemplary Sub-Embodiments

-   -   Wherein said superior properties for desorption include one or         more or a combination of the following: higher gas equilibrium         partial pressure, faster desorption kinetics, greater desorption         of a desired gas relative to a less desired gas, low viscosity,         low volatility of other solvent constituents, low relative         volatility of other solvent constituents, no degradation, no         corrosion, minimal degradation, minimal corrosion, compatibility         with gas impurities, minimal impurities in desorbed gases

Cooling Cloud Point Reagents Exemplary Embodiments

A method for creating reagents blends with upper critical solution temperatures with reagents which may, independently not have upper critical solution temperatures.

A method for creating a reagent mixture that has a cooling solubility swing or upper critical solution temperature or cooling ‘thermally switchable solubility’ or cooling cloud point while maintaining other desirable properties:

-   -   A reagent mixture which forms X+n number of liquid phases upon         cooling below one or more cloud point temperatures comprising         one or more or a combination of the following:         -   Reagent 1: One or more reagents with relatively low             solubility in Reagent 2 and temperature dependent relatively             higher or miscible solubility in Reagent 3.         -   Reagent 2: One or more reagents with relatively low             solubility in Reagent 1 and relatively higher or miscible             solubility in Reagent 3.         -   Reagent 3 one or more reagents comprising one or more or             combination of the following properties:             -   A reagent with high solubility in both Reagent 1 and                 Reagent 2 under certain conditions, which may be the                 same conditions.             -   A reagent with higher solubility or higher affinity or                 more attraction for Reagent 1 than Reagent 2 at                 relatively elevated temperatures or above certain                 relatively elevated temperatures (if cooling cloud point                 is desired).             -   A reagent with higher solubility or higher affinity or                 more attraction for Reagent 2 than Reagent 1 at                 relatively cooler temperatures or below certain                 relatively cooler temperatures (if cooling cloud point                 is desired).

Exemplary Sub-Embodiments

-   -   Wherein Reagent 1 comprises one or more or a combination of the         following: water, ethylene glycol, propylene glycol, glycerol,         organic reagents, inorganic reagents, ammonia     -   Wherein Reagent 2 comprises one or more or a combination of the         following: diethyl ether, dimethyl ether, propylene carbonate,         ethers, glycols, polyethylene glycol dimethyl ether, ethylene         carbonate, organic reagents, inorganic reagents, ammonia     -   Wherein Reagent 3 comprises one or more or a combination of the         following:

polypropylene glycol, polypropylene glycol with one or more molecular weights ranging from 400 g/mole-10,000 g/mole, polyethylene glycol, polyethylene glycol with one or more molecular weights ranging from 200 g/mole-100,000 g/mole, organic reagents, inorganic reagents, ammonia

-   -   Wherein the reagent combination further comprises reagent 4, a         reagent which is soluble in Reagent 1 alone, and exhibits         limited solubility, in Reagent 2, Reagent 3, or both.     -   Wherein the reagent combination further comprises one or more         salts     -   Wherein the biphasic solution comprises one phase composed         primarily of propylene carbonate and another phase composed         primarily of water and polypropylene glycol     -   Wherein the cloud point temperature of the reagent combination         is adjusted by changing the relative concentration of one or         more or a combination of reagents     -   Wherein the cloud point temperature of the reagent combination         is adjusted by changing the relative concentration of one or         more salts in the solution     -   Wherein the cloud point temperature of the reagent combination         is adjusted by changing the composition of the constituent         reagents     -   Wherein the solution comprises a single liquid phases above the         one or more cloud point temperatures and a multiphase solution         below the one or more cloud point temperatures     -   Wherein the solution comprises two liquid phases above the one         or more cloud point temperatures and a three or more-liquid         phase solution below the one or more cloud point temperatures     -   Wherein the solution comprises a X number of liquid phases above         the one or more cloud point temperatures and a X number of         liquid phases below the one or more cloud point temperatures         -   Wherein the composition of one or more of the X number of             liquid phases is different above or below said cloud point             temperature     -   Wherein the solution is mixed to facilitate transitioning toward         the equilibrium state     -   ‘Heating Cloud’ Point Reagents with, for example, Low Viscosity         or Cost or Combination Thereof

Exemplary Embodiments

A method for creating a reagent mixture that has a heating solubility swing or heating ‘thermally switchable solubility’ or heating cloud point while maintaining other desirable properties:

-   -   A reagent mixture which forms X+n number of liquid phases upon         heating above one or more cloud point temperatures comprising         one or more or a combination of the following:         -   Reagent 1: One or more reagents with relatively miscible             solubility in Reagent 2 and high or miscible solubility in             Reagent 3 below a certain temperature range or ranges.         -   Reagent 2: One or more reagents soluble in reagent 1 and 3.         -   Reagent 3: one or more reagents comprising one or more or             combination of the following properties:             -   A reagent with high solubility in both Reagent 1 and                 Reagent 2 under certain conditions, which may be the                 same conditions.             -   A reagent with higher solubility or higher affinity or                 more attraction for Reagent 1 than Reagent 2 at                 relatively elevated temperatures or above certain                 relatively elevated temperatures             -   A reagent with higher solubility or higher affinity or                 more attraction for Reagent 2 than Reagent 1 at                 relatively cooler temperatures or below certain                 relatively cooler temperatures

Exemplary Sub-Embodiments

-   -   Wherein Reagent 1 comprises one or more or a combination of the         following: water, ethylene glycol, propylene glycol, glycerol,         organic reagents, inorganic reagents     -   Wherein Reagent 2 comprises one or more or a combination of the         following: polyethylene glycol dimethyl ether, polyethylene         glycol, polyethylene glycol with one or more molecular weights         ranging from 200 g/mole-100,000 g/mole, glycerol, propylene         glycol, propylene carbonate, ethers, glycols, ethylene         carbonate, organic reagents, inorganic reagents     -   Wherein Reagent 3 comprises one or more or a combination of the         following: polypropylene glycol, polypropylene glycol with one         or more molecular weights ranging from 400 g/mole-10,000 g/mole,         polyethylene glycol, polyethylene glycol with one or more         molecular weights ranging from 200 g/mole-100,000 g/mole,         organic reagents, inorganic reagents     -   Wherein the reagent combination further comprises reagent 4, a         reagent which is soluble in Reagent 1, and exhibits limited         solubility, in Reagent 2, Reagent 3, or both.     -   Wherein the reagent combination further comprises one or more         salts     -   Wherein the cloud point temperature of the reagent combination         is adjusted by changing the relative concentration of one or         more or a combination of reagents     -   Wherein the cloud point temperature of the reagent combination         is adjusted by changing the relative concentration of one or         more salts in the solution     -   Wherein the cloud point temperature of the reagent combination         is adjusted by changing the composition of the constituent         reagents     -   Wherein the solution comprises multiple liquid phases above the         one or more cloud point temperatures and a single liquid phase         below the one or more cloud point temperatures     -   Wherein the solution comprises two liquid phases below one or         more cloud point temperatures and three or more liquid phases         above one or more cloud point temperatures     -   Wherein the solution comprises a X number of liquid phases above         the one or more cloud point temperatures and a X number of         liquid phases below the one or more cloud point temperatures         -   Wherein the composition of one or more of the X number of             liquid phases is different above or below said cloud point             temperature     -   Wherein the solution is mixed to facilitate transitioning toward         the equilibrium state     -   Wherein Reagent 2 has a lower viscosity than Reagent 3.         -   (For Example: Physical or Physio-Chemical Solvent)

Exemplary Embodiments

-   -   (a) A CO₂ physical absorbent comprising:         -   Cation comprising ammonium, alkali, alkaline earth,             transition metal, metal cation, or combination thereof         -   Anion comprising dihydrogen phosphate, or monohydrogen             phosphate, or combination thereof         -   Water, or organic solvent, or combination thereof     -   (b) An acid gas absorbent comprising:         -   Aqueous ammonia or ammonium         -   An ‘Acidic’ Ammonium salt         -   Wherein the pH of the solution is equal to or below 8.8

Exemplary Sub-Embodiments (for Example: Separating Acid Gases)

-   -   (for example, embodiment above) Wherein the pH of the solution         without acid gases is greater than 7         -   (For Example: with Thermally Switchable Stripping Reagent)

Exemplary Embodiments (for Example: Separating Acid Gases, with Thermally Switchable Stripping Reagent)

-   -   (a) A process for separating acid gases comprising:         -   A physical solvent         -   An acidic or ionic reagent         -   Wherein the concentration of the acidic or ionic reagent is             significantly greater in the desorption solution than the             absorption solution     -   (b) A process for separating acid gases comprising:         -   A physical solvent         -   A basic salt         -   An acidic or ionic reagent

Exemplary Sub-Embodiments (For Example: Separating Acid Gases with Thermally Switchable Stripping Reagent)

-   -   Wherein the basic salt solution with a pH of less than 8.8 in         the absence of an acid gas     -   Wherein the basic salt solution with a pH of less than 8.5 in         the absence of an acid gas     -   Wherein the acidic reagent does not undergo a metathesis or         displacement or combination thereof reaction in the presence of         the basic salt     -   Wherein the concentration of the acidic reagent is adjusted         using temperature driven solubility change     -   Wherein the concentration of reagents is adjusted using         temperature driven solubility change, precipitation, acid gas         driven precipitation, membrane-based process, crystallization,         or a combination thereof     -   Wherein the acidic reagent maintains relatively the same         concentration in the absorption solution as the desorption         solution     -   Wherein the basic reagent maintains relatively the same         concentration in the absorption solution as the desorption         solution     -   Wherein the concentration of the acidic or ionic reagent is         greater in the desorption solution than the absorption solution     -   Wherein the concentration of the basic or ionic reagent is         greater in the absorption solution than the desorption solution     -   Wherein the acidic reagent comprises boric acid or one or more         of its derivatives     -   Wherein the basic salt comprises a salt with one or more anions         with a competing reaction to the acid gas     -   Wherein the basic salt comprises a salt with one or more anions         with a competing reaction to the acid gas Wherein one or more         anions have stronger affinity for the one or more cations than         the acid gas     -   Wherein the basic salt facilitates acid gas absorption due to         the basicity of the solution Wherein the basic salt maintains         its integrity in the presence of the acid gas     -   Wherein the basic salt facilitates acid gas absorption due to         the basicity of the solution Wherein the basic salt does not         undergo a metathesis or displacement or carbonation or         combination thereof reaction in the presence of the acid gas     -   Wherein the concentration of basic salt may be adjusted using         temperature driven solubility change

Exemplary Embodiment

-   -   (a) Systems & methods for separating gases comprising:     -   Absorbing one or more gases in one or more physical solvent         liquid phases     -   Wherein said one or more solvent liquid phases is at least one         of two or more liquid phases resulting from an Upper Critical         Solution Temperature (UCST) or a Lower Critical Solution         Temperature (LCST) phase change

Exemplary Sub-Embodiments

-   -   (b) Wherein the phase change occurs during the absorption of one         or more gases     -   (c) Wherein the phase change occurs during absorption         -   Further comprising a LCST phase change which absorbs at             least a portion of the heat of absorption     -   (d) Wherein the phase change occurs during absorption         -   Further comprising a LCST phase change which absorbs at             least a portion of the heat of absorption         -   Further comprising the dissolution of the two or more liquid             phases during desorption, recovering at least a portion the             heat of absorption through the endothermic phase change     -   (e) Wherein the phase change occurs before absorption     -   (f) Wherein the liquid phases are separated using a         liquid-liquid separation device prior to absorption     -   (g) Wherein the two or more liquid phases are separated using         one or more liquid-liquid separation devices     -   (h) Wherein the liquid phases are in single mixture of two or         more liquid phases during gas absorption     -   (i) Wherein the liquid phases are in two or more separate         absorption columns with each absorption column specific to each         liquid phase     -   (j) Wherein the combined liquid solution absorbs gases under         conditions to form two or more liquid phases and desorbs gases         under conditions to form a combined liquid phase     -   (k) Wherein the dissolved gas rich phase, liquid phase 1,         absorbs gas in one or more gas-liquid contactors     -   (l) Wherein another liquid phase, liquid phase 2, is mixed with         dissolved gas rich liquid phase 1 to:         -   a) Reduce dissolved gas solubility         -   b) increase dissolved gas partial pressure         -   c) Provide heat or entropy to facilitate the desorption of             one or more dissolved gases         -   d) Increase the solubility of one dissolved gas relative to             another dissolved gas before desorption of said one             dissolved gas)         -   e) Decrease the solubility of one dissolved gas relative to             another dissolved gas before desorption of said another             dissolved gas         -   f) A combination thereof     -   (m) Wherein one liquid phase functions as an ‘antisolvent’ while         another liquid phase functions as the primary physical absorbent         -   Wherein, upon dissolution of the antisolvent, the combined             solution has a relatively lower solubility of one or more             dissolved gases     -   (n) Wherein one liquid phase is selective for one or more gases         and another liquid phase is selective one or more gases     -   (o) Wherein one liquid phase is selective for one or more gases         and another liquid phase is selective one or more different         gases     -   (p) Wherein one liquid phase is selective for one or more gases         and another liquid phase is selective one or more different         gases         -   Further comprising desorbing one or more gases from one or             more liquid phases before combining the liquid phases     -   (q) Wherein the liquid-liquid separation device comprises one or         more or a combination of the following: decanter, cyclone,         centrifuge, coalescer, filter     -   (r) Wherein the dissolution of one or more liquid phases reduces         the solubility of one or more gases one or more or a combination         of the following: forming a combined solution with a lower acid         gas solubility than the two or more separate phases, increasing         pH, decreasing pH, providing heat before or during desorption         due to the enthalpy of dissolution, providing entropy before or         during desorption due to the entropy of dissolution     -   (s) Wherein one or more of the liquid phases is a physical         solvent, and said physical solvent phase is rich in organic,         organic solvent, organic polymer, or combination thereof     -   (t) Wherein one or more of the liquid phases functions as an         antisolvent,′ and said antisolvent phase is rich in water, one         or more ionic compounds, one or more relatively lower acid gas         solubility reagents, or a combination thereof     -   (u) Wherein the liquid phases exhibit similar solubility of one         or more gases     -   (v) Where said two or more liquid phases exhibit different         solubility of one or more gases

Exemplary Embodiment

-   -   (w) Absorbing two or more gases in a combined or single liquid         phase         -   Further comprising forming two or more liquid phases from             the single liquid phase resulting from a UCST or LCST phase             change         -   Wherein at least one liquid phase possesses desirable             properties for one or more dissolved gases

Exemplary Sub-Embodiments

-   -   (x) Wherein one or more other liquid phases possess desirable         properties for one or more different dissolved gases than said         dissolved gases for which liquid phase 1 possesses desirable         properties     -   (y) Wherein one or more of said liquid phases comprise physical         solvents     -   (z) Wherein said desirable properties include one or more or a         combination of the following: selectivity for one more gases         relative to one or more gases compared to the other liquid         phase, higher concentration of one more gases relative to one or         more gases compared to the other liquid phase, greater         desorption kinetics for one or more gases compared to the other         liquid phase, greater equilibrium partial pressure of one or         more gases in one liquid phase compared to the other liquid         phase, lower energy of regeneration of one or more gases         compared to the other liquid phase, desirable properties for         reacting one or more gases in one liquid phase relative to         another liquid phase, desirable properties for liquifying one or         more gases relative to another liquid phase, higher gas         equilibrium partial pressure, faster desorption kinetics,         greater desorption of a desired gas relative to a less desired         gas, low viscosity, low volatility of other solvent         constituents, low relative volatility of other solvent         constituents, no degradation, no corrosion, minimal degradation,         minimal corrosion, compatibility with gas impurities, minimal         impurities in desorbed gases     -   (aa) Wherein the one or more gases are desorbed from their         specific liquid using means specific for the one or more gases         targeted for desorption     -   (bb) Wherein the solubility of one or more dissolved gases in         the combined liquid phase is greater than the solubility of one         or more of said dissolved gases in one or more of the separate         liquid phases

Exemplary Embodiment

-   -   (cc) Absorbing one or more gases in a physical solvent, forming         a dissolved gas rich physical solvent comprising one or more         dissolved gases and physical solvent         -   Combining said dissolved gas rich physical solvent with an             antisolvent, forming a gas rich combined solution         -   Desorbing said one or more dissolved gases from said gas             rich combined solution, forming a dissolved gas lean             combined solution         -   Regenerating the antisolvent and physical solvent solutions             from said gas lean combined solution using one or more or a             combination of membrane-based processes

Exemplary Sub-Embodiments

-   -   (dd) Wherein said physical solvent comprises a liquid with a         molar mass below the molecular weight cutoff of the membrane or         membranes employed to separate the antisolvent reagents from the         physical solvent     -   (ee) Wherein said physical solvent comprises one or more or a         combination of the following: liquid with a molecular weight         below the molecular weight cutoff of one or more membranes         employed herein, water, organic solvent, non-volatile organic         solvent, propylene glycol, ethylene glycol, propylene carbonate,         ethylene carbonate, glycerol, urea     -   (ff) Wherein said antisolvent increases the pH to facilitate the         desorption of one or more basic gases     -   (gg) Wherein said antisolvent decreases the pH to facilitate the         desorption of one or more acid gases     -   (hh) Wherein interactions of said antisolvent with said         dissolved gases are reversible using membrane separation     -   (ii) Wherein said antisolvent reagent solvent comprises one or         more reagents in the physical solvent     -   (jj) Wherein said antisolvent further comprises one or more         other reagents dissolved in said solvent     -   (kk) Wherein said mixed solution is regenerated into physical         solvent and antisolvent using reverse osmosis, nanofiltration,         ultrafiltration, forward osmosis, membrane distillation, or a         combination thereof     -   (ll) Wherein said mixed solution is regenerated into physical         solvent and antisolvent using reverse osmosis, nanofiltration,         ultrafiltration, forward osmosis, membrane distillation, or a         combination thereof     -   (mm) Wherein said antisolvent comprises a ‘concentrate’ and said         physical solvent comprises a ‘permeate’     -   (nn) Wherein said antisolvent reagent increases the solubility         of one or more dissolved gases relative to one or more different         dissolved gases     -   (oo) Wherein said antisolvent reagent decreases the solubility         of one or more dissolved gases relative to one or more different         dissolved gases     -   (pp) Wherein the antisolvent is enriched with one or more         dissolved gases relative to the total solubility of said gases         in said antisolvent     -   (qq) Wherein the antisolvent contains one or more reagents with         a molecular weight greater than the molecular weight cutoff of         the membrane or membranes employed to separate the antisolvent         reagents from the physical solvent     -   (rr) Wherein the antisolvent contains one or more reagents         capable of being rejected by a membrane or membranes employed to         separate the antisolvent reagents from the physical solvent     -   (ss) Wherein the antisolvent comprises one or more or a         combination of the following: acid, organic acid, inorganic         acid, acid with a hydration radius greater than 80da, organic         acid with a hydration radius greater than 80da, polymer, acidic         polymer, ionic compound, acidic ionic compound, weak base—strong         acid, cation-hydrogen or dihydrogen-anion or trihydrogen-anion         salt, alkali hydrogen sulfate salt, ammonium—strong acid salt,         common-ion salt, citric acid, water, organic solvent     -   (tt) Wherein the antisolvent comprises one or more or a         combination of the following: base, amine, imine, azine, organic         base, inorganic base, strong base, base with a hydration radius         greater than 80da, organic base with a hydration radius greater         than 80da, polymer, basic polymer, ionic compound, basic ionic         compound, strong base—weak acid, common-ion salt water, organic         solvent     -   (uu) Wherein the solubility of one or more gases in the combined         solution is less than the solubility of one or more gases in one         or more of the individual liquid phases     -   (vv) Wherein the solubility of one or more gases in the physical         solvent is greater than the solubility of one or more gases in         the antisolvent     -   (ww) Wherein said physical solvent may contain antisolvent,         including, but not limited to, as an impurity     -   (xx) Wherein said gases comprise one or more or a combination of         the following: acid gases, basic gases, hydrocarbons, inert         gases, air

Further Descriptions of Above Embodiments

Note:

The one or more temperatures of the cloud point or cooling cloud-point and the relative volumes or masses of the one or more cloud-point phases may be adjusted by changing the relative concentrations and types of one or more reagents.

Note:

The one or more cloud-point temperatures of one or more liquid systems may be tuned to any temperature by, for example, including, but not limited to, one or more or a combination of the following: increasing or decreasing the concentration of one or more reagents, or additives that decrease cloud point temperature (for example: salts, certain organic reagents) or additives that increase cloud point temperature (for example: certain organic reagents) or combination thereof.

Mild temperatures required to reach one or more cloud point temperatures may be supplied from, including, but not limited to, one or more or a combination of the following: heat pump, waste heat source, condenser water, cooling water waste heat, cooling air waste heat, solar heat, or other heat source.

Note:

One or more absorption solutions may be a multi-liquid phase mixture before absorption.

Note:

Alternatively, if, for example, there may be no or minimal dissolved gas partial pressure swing, phase change solution may provide significant benefits which may include, but are not limited to, one or more or a combination of the following: cooling the absorber, providing a smaller temperature profile in the absorber, preventing the need for external cooling in the absorber or recovering the enthalpy of absorption, or providing entropy or heat release during desorption.

Note:

One or more dissolved gases in a dissolved gas rich combined solution may possess different concentrations in one or more liquid phases, than, for example, one or more other liquid phases. Said liquid phases may be in said combined solution and/or may form from one or more phase transitions. For example, one gas may have a significantly higher concentration in one liquid phase than another liquid phase. For example, if two liquid phases may be liquid phase A and B, respectively, one gas may have a significantly higher concentration in liquid phase A than liquid phase B and another gas may have a significantly higher concentration in liquid phase B than liquid phase A. Alternatively, for example, one gas may have a significantly different concentration in liquid phase A relative to liquid phase B and another gas may have a similar concentration in both liquid phases. Alternatively, for example, liquid phase A may have more desirable properties for desorbing or recovering said one or more gases or liquids from solution than liquid phase B. Alternatively, for example, the one or more gases may have similar concentration in liquid phase A as liquid phase B, although liquid phase B may have superior or more desirable properties for desorbing or recovering said one or more gases or liquids from solution.

Note:

In some embodiments, the physical solvent or adsorbent may be separated from the liquid using a solid-liquid separation device. This may be the case, for example, if a solid absorbent that is thermally switchable is employed. For example, diammonium phosphate, as a basic salt, may function as a solid adsorbent. Another example may be, for example, a solid polymer which may be water or liquid soluble under some conditions and water or liquid insoluble under other conditions (Note: Said water may alternatively constitute an organic solvent or non-aqueous phase or a combination thereof).

Note:

Figures may show ‘acid gases’ as being separated. In said figures, Acid Gases may be provided as an example desired gas or dissolved gas or example gas to be separated or removed. Other gases, including, but not limited to, other gases described herein, may be separated in said Figures or embodiments.

Note:

When physical solvent may be highly concentrated or water-lean or water-free, it may exhibit relatively high solubility of one or more gases (for example: >2 g CO₂ per liter of solvent at 20° C. and atmospheric pressure), which may be comparable to, for example, other physical solvents. When the physical solvent may be mixed with an antisolvent (such as an aqueous solution or aqueous salt water solution), the solubility of one or more gases may significantly decrease and the equilibrium partial pressure of said one or more gases may significantly increase. For example, the solubility of acid gas in the resulting aqueous solution may be greater than water. Lower solubility than in organic physical solvent alone or equal to or less than the solubility of acid gas in water at the same temperature. Said physical solvent, after acid gas desorption, may be regenerated through one or more methods described herein.

Note:

The ratio of physical solvent to antisolvent may be determined based on the solubility of one or more desired gases in one or more physical solvent phase, the solubility of one or more gases in one or more antisolvent phases, and the solubility of one or more gases in solutions comprising a combination thereof. The amount of antisolvent may be sufficiently significant relative to physical solvent to decrease the solubility of one or more gases in the resulting solution, however not significant enough that it dilutes the concentration of one or more dissolved gases in the combined solution to the point where the net solubility of one or more dissolved gases may be, for example, equal to or less than the total solubility of gas in said physical solvent. It is important to note that said anti-solvent may or may not be saturated with one or more desired gases before being mixed with said physical solvent.

Note:

One or more absorption units may operate at an equal or different pressure than one or more desorption units. For example, one or more absorption units may operate at a higher pressure to, for example, increase the solubility of one or more gases.

Note:

The mere presence of an acidic reagent in solution may significantly reduce the solubility of an acid gas relative to a physical solvent without an acidic reagent. Similarly, the mere presence of a basic reagent in solution may significantly reduce the solubility of a basic gas relative to a physical solvent without a basic reagent.

Note:

Reverse osmosis, nanofiltration, forward osmosis, and/or other membrane-based processes may enable the an absorption solution with minimal or practically no reagents which are meant to suppress the solubility of one or more desired gases and may enable the introduction of one or more reagents which are meant to suppress the solubility of one or more desired gases for desorption. Said membrane-based processes may exhibit high selectivity and/or relatively low energy consumption relative to some other liquid separation processes.

Note:

For example, an easily separable stripping gas may be, for example, a gas that may possess, including, but not limited to, one or more or a combination of the following: minimally dissolves or practically does not dissolve in one or more solutions being ‘stripped,’ separable from the other gases using one or more gas membranes, separable from the other gases using condensation, separable from the other gases using compression, separable from the other gases using a reversible reaction, or separable from the other gases.

Note:

The concentration of other air components, including, but not limited to, argon, carbon dioxide, water vapor, methane, may be selectively absorbed, desorbed, or concentrated during the one or more liquid-liquid phase changes.

Note:

To, for example, optimize cloud-point temperature and/or other separation properties (for example, including, but not limited to, liquid-liquid phase separation, layer separation, liquid phase composition, liquid phase distribution, or combination thereof), one or more liquid phases may include one or more additives, such as, for example, salts and organic reagents. Said additives may decrease or increase cloud-point temperature or improve phase separation properties or adjust organic reagent osmotic pressure (may be, for example, applicable in versions of one or more embodiments employing reverse osmosis, nanofiltration, or ultrafiltration to concentrate, for example, one or more salts or selectively concentrate one or more organic reagent, selectively concentrate one or more inorganic reagents, or to selectively not concentrate one or more salts or organic reagents or inorganic reagents, or a combination thereof).

Note:

LLS-1 may comprise one or more liquid-liquid separators or separation devices (which may include, but not limited to, one or more or a combination of the following: cyclone, centrifuge, coalescer, decanter, or filter).

Note:

Acid gases may include, but are not limited to, one or more or a combination of the following: CO₂, H₂S, HF, SO₂, NO₂, HCN, HCl, HI, HBr.

Note:

One or more desired gases may be in gas streams with one or more or a combination of other gases.

Note:

Systems, methods, embodiments, or combinations thereof described herein may be employed for separating gases or liquids. Embodiments described herein may, for example, separate two or more gases with different solubilities in one or more of the solvents employed in the technology. For example, one or more embodiments may be employed for separating basic gases, such as ammonia. Alternatively, for example, one or more embodiments may be employed to separate hydrocarbons from inert gases (for example: N₂, O₂, Argon) or from other hydrocarbons or from a combination thereof. One or more hydrocarbons may, for example, have a higher solubility than one or more other gases, such as inert gases, in, for example, one or more the physical solvents. Then, for example, said one or more physical solvents may be mixed with one or more antisolvents, for example, which may include, but are not limited to, a salt water solution, resulting in the desorption or phase separation of said one or more hydrocarbons as gases or as liquids.

Note:

A reduction in pH may facilitate acid gas desorption. An increase in pH may facilitate basic gas desorption.

Note:

A method for creating a liquid system exhibiting one or more phase transitions, while maintaining other desirable properties, which may include, but are not limited to, low viscosity or higher purity of physical solvent, may comprise reagents with, for example, including, but not limited to, one or more or a combination of the following properties:

-   -   Reagent 1: A reagent with relatively low solubility in Reagent 2         and relatively higher or miscible solubility in Reagent 3.     -   Reagent 2: A reagent with relatively low solubility in Reagent 1         and relatively higher or miscible solubility in Reagent 3.     -   Reagent 3 comprises one or more or combination of the following         properties:         -   A reagent with high solubility in both Reagent 1 and Reagent             2 under certain conditions, which may be the same             conditions.         -   A reagent with higher solubility or higher affinity or more             attraction for Reagent 1 than Reagent 2 at relatively             elevated temperatures or above certain relatively elevated             temperatures (if cooling cloud point is desired).         -   A reagent with higher solubility or higher affinity or more             attraction for Reagent 2 than Reagent 1 at relatively cooler             temperatures or below certain relatively cooler temperatures             (if cooling cloud point is desired).     -   Reagent 4: A reagent which is soluble in Reagent 1 alone, and         not soluble, or exhibits limited solubility, in Reagent 2,         Reagent 3, or both.

Note:

Alternative basic salt solutions for physical absorption or quasi-physical absorption may include, but are not limited to, one or more or a combination of the following: CO₂-Rich aqueous ammonia, sodium carbonate solutions, sodium sesquicarbonate solutions, sodium carbonate-bicarbonate solutions, alkali carbonate-bicarbonate solutions, acidic salt-ammonia solutions (for example, including, but not limited to, ammonium sulfate-ammonia, ammonium nitrate-ammonia, ammonium chloride-ammonia).

Note:

One or more solutions may contain aqueous ammonia. If one or more solutions contain aqueous ammonia, it may be desired for the concentration of ammonia in the solution or other reagents in said one or more solutions enable the solution to be at a pH below the pH of free ammonia (below ˜8.5 or below ˜9), although at a basic pH (for example: >pH of 7).

Note:

A gas blower or compressor (‘Gas Compressor’) may be employed.

Note:

A portion of water vapor may be removed from the one or more desorbed gas streams or one or more gases stream exiting one or more absorption units or a combination thereof. Said water vapor removal may be employed, for example, before or after entering one or more gas compressors, using, for example, one or more water removal methods, including, but not limited to, one or more or a combination of the following: cooling condensers or desiccants. Water vapor may be removed, to, for example, including, but not limited to, one or more or a combination of the following: reduce corrosion, prevent accumulation of water in absorption solution (or otherwise ensure proper water balance), or reduce the energy required to compress or otherwise transfer one or more gases. For example, a cooling condenser may be employed, wherein, for example, one or more gas streams may be cooled to 0-5° C., reducing the water vapor concentration to below 1 vol % through condensation. G-2 may represent a pressurized, water-lean gas stream.

Note:

One or more gases remaining after, for example, absorption may undergo further scrubbing or treatment (for example, in embodiments employed for acid gas removal: employing a deep scrubbing method, such as employing a strong base—for example sodium hydroxide, or high absorption efficiency absorbent or adsorbent, such as an amine or quaternary ammonium compound). Said further treatment may be beneficial, for example, in one or more embodiments where one or more gases are removed from one or more valuable gas streams (for example: removal of CO₂ from biogas or natural gas to increase the concentration of potentially more valuable methane) or one or more gases are valuable gas streams, which may require for said one or more valuable gases to reach certain purity levels.

Note:

Cooling may be conducted during, for example, before or during or after the absorption of one or more gases. Said cooling may be employed, for example, to ensure the solution remains at an appropriate temperature and/or remove heat due to the enthalpy of absorption. Said cooling input may involve the use of, including, but not limited to, cooling water, heat sink, chiller or other cooling source or sources or combination thereof.

Note:

Heat sources may include one or more or a combination of heat sources known in the art, which may include, but are not limited to, one or more or a combination of the following: waste heat, condenser water, cooling water waste heat, steam, heat pump, solar heat, or other heat source.

Note:

A heat pump may be employed to provide, for example, simultaneous heating and cooling required for, for example, temperature driven thermal switching or precipitation. Thermal switching or precipitation generally may involve an endothermic or exothermic phase change, wherein, for example, the enthalpy of precipitation or thermal switching may be largely similar to the enthalpy of dissolution or mixing. As a result, one or more heat pumps may extract heat from one or more exothermic steps and provide said heat for one or more endothermic steps.

Note:

An increase acidic salt concentration may reduce pH and may, for example, increase the partial pressure of one or more acid gases (for example: CO₂, H₂S, HCN, HF, SO₂, NO₂).

Note:

The aqueous solution may function as a physical solvent. In, for example, the embodiment shown in FIG. 2A, one or more liquid phases possessing higher solubility of one or more gases may be considered a physical solvent, even though, for example, one or more lower CO₂ or acid gas solubility liquid phase may possess CO₂ solubility.

Note:

FIG. 7A-7C may show an example embodiment where M-1 and M-2 (acidic or basic reagent ‘precipitation or thermal switching’ or ‘dissolution’ vessels) may be run in opposing sequence. For example, when M-1 may be precipitating or thermal switching acidic reagent from an acidic reagent—Rich, acid gas-Lean solution, M-2 may be dissolving acidic reagent into an acidic reagent—lean, acid gas-Rich solution.

Note:

One or more embodiments described herein may employ a flash desorber which may desorb one or more dissolved gases due to depressurization. In some embodiments, in may be desirable to recycle at least a portion of said desorbed gas to one or more absorption units. For example, said recycle may be employed in an embodiment employed for acid gas removal, for example, if there may be residual methane or other contaminants in said recycled gas stream requiring further treatment or separation.

Note:

An example solvent may comprise, for example, an aqueous solution of diammonium phosphate, aqueous ammonia, a combination thereof, or another relatively basic pH fertilizer. Some embodiments, for example, may be employed to remove CO₂ from biogas produced, for example, on a farm. CO₂ in biogas may be absorbed into, for example, a diammonium phosphate solution employed on the farm as a fertilizer. The remaining ‘non-CO₂’ gases (for example: Biomethane) may be, for example, injected into a natural gas grid, undergo further treatment before injection into a natural gas grid, undergo further treatment, or may be used for one or more biomethane applications. The resulting CO₂-Rich fertilizer solution may simply be employed as a fertilizer as, for example, it may have otherwise, eliminating the need for, for example, a desorption column or desorption step within the biogas upgrading process.

Note:

Upgraded biogas or natural gas or other gas stream may undergo additional treatment, for example, may include, but is not limited to, removal of a portion of water vapor.

Note:

In the case of precipitation: After precipitation and draining or separation of the solution from the precipitate, M-1 (now containing precipitate) may now become the precipitate dissolution vessel, while M-2 becomes the cooling precipitation vessel. The precipitate may not require transfer from the vessel, minimizing precipitate handling challenges. During the precipitation and dissolution, M-1 and M-2 may be heat exchanged through, for example, exchanging jacketed vessel liquids (for example: water, or silicone oil), and may be further accelerated or enhanced using, for example, a heat pump. The heat of precipitation is similar to the heat of dissolution, thus heat exchanging these two stages may reduce energy requirements.

Note:

In the case of thermal switching: The thermally switched (either through heating or cooling) phases may be separated. In the case of liquids, said separated liquids may be transferred to their respective next steps. Due to the ability to transport liquids using one or more pumps, one or more liquids may be stored or transferred to in excess capacity vessels to ensure there is sufficient amounts available to ensure the plant can keep running, at least temporarily, if a problem occurs.

Note:

In the case of an endothermic phase separation or clouding or LCST, the phases may be clouded out before or during the absorption of one or more gases and may be mixed or dissolved before or during desorption of one or more gases. In the case of an exothermic phase transition or clouding or UCST, one or more phases may be phase transitioned before or during the desorption of one or more gases and may be mixed or dissolved before or during the absorption of one or more gases.

Note:

Embodiments herein may employ pumps or other fluid or mass transfer devices. Figures may not include all necessary pumps and other devices. For example, there are numerous configurations and types of pumps that may be employed in the embodiments described herein.

Note:

A reagent blend comprising Basic Salt (for example: one or more or a combination of dihydrogen phosphate salts)+Water+Organic Reagent (for example: one or more or a combination of non-volatile organic solvents or polymers) may possess a relatively high CO₂ solubility (For example: >0.7 g CO₂ per 100 g solution at 30 PSI CO₂ partial pressure at 25° C.) as a combined solution, as two or more separated phases (for example: ‘clouded-out’ or ‘thermally switched’), or a combination thereof. The reagent combination described thereof may be applicable to, for example, one or more or a combination of embodiments herein, including, but not limited to, FIG. 1. In the case of employing said reagent blend in FIG. 1, the process may benefit from the recovery of the enthalpy of absorption of acid gas (removing heat during absorption as one or more phases ‘cloud-out’ from solution from, for example, the temperature rise) and the subsequent release of heat and entropy during the dissolution of the ‘clouded-out phases’ during the desorption of acid gas.

Note:

The basic salt solution, which may be employed in the embodiments shown in FIGS. 6 and 7, may absorb one or more gases, such as acid gases or CO₂, by including, but not limited to, one or more or a combination of the following: physical or physio-chemical manner. The basic solution reagent may include, but is not limited to, salts that form basic solutions with water, however may maintain composition in the presence of CO₂ or one or more other acid gases. The cation or cations of one or more salts may have a higher affinity for the pre-existing anion or anions it/they is/are bonded to than CO₂(aq) or other dissolved acid gases or combination thereof. An example salt may be diammonium phosphate, which forms a basic solution with water. Aqueous solutions of diammonium phosphate (DAM) may exhibit an appreciably higher solubility of CO₂ in than deionized water. DAM(aq) may exhibit a 3-6.5× greater CO₂ solubility or greater CO₂ solubility per kilogram of solution than deionized water.

Note:

If one or more liquid phases re-dissolve or re-combine or form more liquid phases or conduct another form of phase transition during absorption, which may form, for example, a solution with less phases or different phases, due to, for example, the heat released during absorption or heat form the surrounding environment or combination thereof, said phase-change reagents may have caused enabled the column to maintain a more stable temperature profile. To achieve a similar average temperature profile using a conventional physical solvent, the physical solvent may have to be cooled significantly below the desired average column or solvent temperature (for example: 5-10° C.), which may require a parasitic form of cooling or may involve less efficient absorption due to average column or solvent temperature in the absorber.

Note:

If desired, a portion of said two or more liquid phases may, for example, in part or in whole, dissolve during absorption, an endothermic phase change which may absorb heat from the absorption column and cool the absorber. Said endothermic dissolution may enable reduced chilling requirements of, for example, the gas stream entering one, or more absorbers or one or more absorbers themselves, or a combination thereof.

Note:

Desired gases may be gases desired to be removed from the gas stream or stream entering the absorber. For example, the desired gases may be acid gases in biogas or natural gas.

Note:

Phase change may occur to one or more other properties in addition to or separate from or without LCST or UCST phase change. For example, including, but not limited to, one or more or a combination of the following: changes in temperature driven solubility without LCST or UCST, changes in light, changes in pressure, changes in the presence of one or more reagents, changes in the concentration of one or more reagents, membrane based separation process, presence of an equilibrium shifting reagent, change in concentration in an equilibrium shifting reagent, changes in sound, or changes in system conditions.

Note:

A liquid solution may have both a UCST and an LCST. For example, a solution may form a multiphase solution or solution of different phase compositions below a certain temperature range and/or above a certain temperature range. Said solution may form a single liquid phase or a less liquid phases between these upper and lower temperature ranges.

Note:

One or more solubility changes may occur due to cooling. For example, below a temperature range or certain temperature points or a certain temperature, the solubility one or more components of the solution may become less soluble and form one or more separate liquid phases.

Note:

Phosphoric acid (2) salts may react with acid gases to form ammonium-phosphates with a lower ratio of ammonia to phosphoric acid (for example: monoammonium phosphate) and a carbon dioxide species salt (for example: ammonium carbamate or ammonium carbonate). Upon one or more changes in conditions (for example: reducing pressure, increasing temperature, or increasing the presence of a reversible equilibrium-shifting reagent [for example: a solubility swing acidic reagent]), CO₂ or another acid gas may desorb, while said phosphoric acid (2) salt may be re-created or regenerated.

Note:

One or more embodiments may employ one or more solid-liquid separation device. For example, FIG. 7A-C may employ one or more solid-liquid separated devices (which may be located internally within M-1 and M-2, as, for example, the precipitate remains in M-2 while the remaining solution exits as L-12). For example, acidic reagent(s) or (l) or (solid-liquid) may remain in M-2 until it is switched to ‘step 2.’

Note:

One or more of the embodiments described herein may be employed to separate organic solvent vapors or other VOCs from gas mixtures.

-   -   For example: The vapor of one or more organic solvents or other         liquids or gases may be soluble in ‘Reagent 1’, which may have         condition sensitive solubility change (for example: UCST or LCST         phase change) in another reagent, Reagent 2. The one or more         organic solvent vapors may be dissolved in, for example, the         combined solution comprising Reagent 1 and Reagent 2. Said         combined solution may comprise a relatively low vapor pressure         of one or more organic solvents due to, for example, including         but not limited to, Reagent 1 functioning as a surfactant. Upon         condition sensitive solubility change of Reagent 1, the reagents         may form two or more separate liquid phases. Reagent 1 rich         phase may become ‘rich’ in one or more organic solvents,         enabling, for example, lower energy or otherwise facilitating         the desorption or distillation or other separation of the         recovered organic solvent. Alternatively, or additionally, one         or more organic solvents in said Reagent 2 rich phase may have         lower solubility or may be saturated or supersaturated,         enabling, for example, lower energy separation of one or more         organic solvent vapors from Reagent 2.     -   Alternatively, or additionally, Reagent 1 may possess greater         solubility of one or more organic solvent vapors relative to         Reagent 2 and Reagent 2 may possess greater solubility of one or         more organic solvent vapors than Reagent 1. Upon liquid phase         change into separate liquid phases, the Reagent 1—rich liquid         phase may be rich in one or more organic solvents or other         reagents and the Reagent 2—rich liquid phase may be rich in one         or more different organic solvents or other reagents. As a         result, the one or more organic solvents may be selectively         separated.     -   For example: The one or more organic solvent vapors or other         liquids or gases may be soluble in ‘Reagent 1’, which may         possess condition sensitive solubility change (for example: UCST         or LCST phase change) or may be separated using a membrane or a         combination thereof from in another reagent or reagents, for         example, Reagent 2. One or more organic solvent vapors or other         liquids or gases may be insoluble or exhibit limited solubility         in Reagent 2. One or more organic solvent vapors may be absorbed         or dissolved in the ‘Reagent 1’ rich phase, which may form a         ‘Reagent 1’ rich phase rich in one or more organic solvents.         Said organic solvent-rich, ‘Reagent 1’-rich phase may be         combined with a ‘Reagent 2’ rich phase. The solubility may         decrease or vapor pressure may increase of the one or more         organic solvents with, for example, the dissolution of the         ‘Reagent 2’ rich phase. One or more organic solvents may be more         easily separated or regenerated from the combined solution         relative to ‘Reagent 1’ rich phase alone. For example, the one         or more organic solvents may be separated using, for example,         including but not limited to, one or more or a combination of         the following: decanting or other liquid-liquid separation of         one or more organic solvent liquid phases that may form upon or         following the dissolution of ‘Reagent 2’ rich phase,         distillation, mechanical vapor compression distillation,         stripping, or a combination thereof.

Note:

M-1 and M-2 may be cooled or heating using one or more cooling or heating methods or using a heat pump interconnected to or heat exchanging between M-1 and M-2. In FIG. 7A-C, M-1 and M-2 may be switched from being dissolution vessels to precipitation vessels and vice versa. To ensure effective heat exchanging and continuous operation, M-1 and M-2 may be operated in opposition (if M-1 is dissolving acidic reagent(s), M-2 may be precipitating acidic reagent(s) and if M-2 is dissolving acidic reagent solid(s), M-1 is precipitating acidic reagent solid(s)).

Note:

One or more embodiments may employ one or more reagents at a concentration where, for example, the osmotic pressure of one or more reagents in one or more solutions or one or more solutions may be sufficiently low such that, for example, one or more solutions may be concentrated using a reverse osmosis or forward osmosis (for example, including, but not limited to, less than 120 bar osmotic pressure for high pressure reverse osmosis, less than 80 bar osmotic pressure for practical high pressure reverse osmosis, or less than 50 bar osmotic pressure for standard reverse osmosis). Said concentrating may be beneficial, as it may reduce or eliminate the need to remove water vapor from the incoming acid gas before it enters the process, reducing OPEX and CAPEX. It may also enable said process to be a net water producing process. Said process may involve a reverse osmosis or other membrane-based process concentrating step or dewatering step, or combination thereof.

Note:

Embodiment may alternatively employ a heat exchanger instead of a heat pump or may not require additional heat input during CO₂ (or other acid gas) stripping.

Note:

An ammonia abatement cycle may be unnecessary or superfluous in one or more embodiments

Note:

One of the functions of two or more absorption units may be to ensure both phases, the low gas solubility phase (for example: salt water aqueous solution) and the high gas solubility phase (for example: the organic physical solvent—rich phase), are nearly saturated with gas. If a low gas solubility phase (for example: salt water aqueous solution) may not be saturated or appreciably enriched with one or more desired gases, when said low gas solubility phase may be mixed with a high gas solubility phase, said low gas solubility phase may more dilute said high gas solubility phase, which may result in a reduced effect of said mixing in shifting equilibrium gas partial pressure. The two or more separate absorption columns may ensure both liquid phases are appreciably enriched in gas before gas desorption, addressing the previously described potential performance inhibitor.

Note:

Alternative basic salt solutions for physical absorption or quasi-physical-chemical absorption include, but are not limited to, one or more or a combination of the following: acidic salt-ammonia solutions, ammonium sulfate-ammonia, ammonium nitrate-ammonia, ammonium chloride-ammonia, diammonium phosphate, mixtures of diammonium phosphate and monoammonium phosphate, sodium phosphate dibasic, potassium phosphate dibasic, calcium phosphates, alkali phosphates, strong base-weaker acid salts, stronger base-weaker acid salts.

Note:

The benefits of an aqueous ammonia-acid ammonium salt solution for acid gas separation, may include, but are not limited to, one or more or a combination of the following:

-   -   Higher absorption capacity at lower acid gas partial pressures         than in physical solvents     -   Lower enthalpy of desorption than regular aqueous ammonia     -   ‘Ammonia’ may be at least partially neutralized by the acidic         ammonium salt, enabling it to be ionic in solution. The         ‘ammonia’ has the benefits of being ionic (for example: minimal         ammonia slip or volatility, competing reaction facilitating acid         gas desorption), however can absorb acid gas despite being ionic         (because, for example, the pKa of the acidic gases in solution         may be stronger than the acidic ammonium salt).     -   No ammonia slip     -   May facilitate precipitation of ammonium bicarbonate     -   Fully reversible     -   Low cost     -   Compatible with many impurities

Note:

CO₂-Rich aqueous ammonia, sodium carbonate solutions, sodium sesquicarbonate solutions, sodium carbonate-bicarbonate solutions, alkali carbonate-bicarbonate solutions

Note:

CO₂ may be recirculated as a ‘stripping gas’ to facilitate, for example, CO₂ desorption in one or more desorption units. For example, a portion of desorbed CO₂ gas stream exiting the desorber may be compressed and fed into the bottom or a low section of the desorber. The solution may be agitated or heated if desired to facilitate desorption.

Note:

changing one or more or a combination of process conditions, including, but not limited to, concentration, temperature, solubility, pressure, light, radiation, ultrasound, or vibration.

Note:

To, for example, facilitate dissolution, a multi-liquid phase mixture exhibiting, for example, one or more LCSTs, may be cooled during dissolution.

Note:

Phase change physical absorbent or Phase change physical absorbents or Phase change physical solvents.

Note:

Liquid with one phase predominately larger or of greater volume or of greater mass than another phase

Note:

The liquid system may comprise the working fluids employed in one or more components of, for example, one or more embodiments described herein, or one or more systems and methods combined herein. Furthermore, a liquid system may comprise the combined reagents which may result in a solution or multi-liquid phase mixture which may possess a phase transition or cloud point or UCST or LCST.

Note:

Further heating or cooling may be required to overcome any losses.

Note:

One or more embodiment may alternatively employ one or more heat exchanger instead or in addition to one or more heat pumps. One or more embodiment may require additional heat input before or during the desorption of one or more gases.

Note:

One or more embodiments described herein may be employed to separate basic gases. For example, Embodiment 9A-C may employ a basic antisolvent, such as, for example, a solution containing an amine or potassium carbonate. Said reagents may reduce the solubility of aqueous ammonia relative to, for example, a solution with just water, such as a solution comprising solely water and dissolved ammonia. Alternatively, said solution may comprise a solution with an acidic salt, such as ammonium nitrate, which may increase the solubility of one or more basic gases in a solution. Said solution without another basic compound or with minimal amounts of basic compound may comprise the physical solvent employed to absorb ammonia from an ammonia laden gas stream. The solution concentrated in one or more other basic compounds may comprise the antisolvent. Combining said antisolvent with said physical solvent may result in a single solution with lower aqueous ammonia solubility or faster aqueous ammonia desorption kinetics or a combination thereof. The aqueous ammonia may be desorbed from said combined solution using, for example, carrier gas stripping, steam stripping or other desorption or recovery method. After ammonia desorption, the ammonia-lean combined solution may be regenerated into the physical solvent and the antisolvent using a membrane-based process, such as reverse osmosis, which rejects the one or more antisolvent reagents, while allowing water and residual ammonia to pass through as permeate. This may result in an antisolvent concentrate solution and a physical solvent permeate solution. The one or more antisolvent reagents may require a hydration radius sufficiently large to be rejected by the one or more membranes. The one or more physical solvent reagents may require a hydration radius or molecular weight sufficiently small to pass through the one or more membranes. The antisolvent-ammonia or antisolvent-dissolved gas or antisolvent-physical solvent, or combination thereof interaction or interactions may desirably be reversible using a membrane-based process.

The concentration of one or more gases in one or more liquid phases or one or more liquid systems may influence one or more UCSTs or LCSTs or combination thereof.

Note:

Other membrane-based processes include Electrodialysis, Reverse Electrodialysis, gas permeable membranes

Note:

An ammonia abatement cycle may be unnecessary

Note:

Example composition:

LCST: propylene carbonate, water, PPG 425, and salt

UCST: propylene carbonate, water, PPG 425

The concentration ratios in the LCST case are ˜25 wt % propylene carbonate, ˜25 wt % PPG 425, and ˜50 wt % aqueous salt solution

The concentration ratios in the UCST case are ˜60 wt % propylene carbonate, ˜15 wt % PPG 425, and ˜25 wt % water

Note:

Strongly acidic solutions employed as, for example, an antisolvent, may be, for example, buffered to a slightly higher pH to ensure the acidic solution is compatible with, for example, the membranes and membrane-based processes that may be employed. For example, an aqueous solution of NaHSO₄ alone may have a pH as low as 1. A ‘buffered’ version of is solution may, for example, contain more sodium cations, using, for example, sodium hydroxide. A ‘buffered’ version of this solution, may possess a pH of, for example 2-3.5.

Note:

wherein said antisolvent may be regenerated from solution using a LCST or UCST or other liquid phase transition, wherein, for example, at least one of the resulting liquid phases comprises, at least in part, an antisolvent

Note:

the desorption stage may desorb gases with from a different number or composition of physical liquid phases than the absorption stage.

Note:

Polypropylene carbonate, polyethylene carbonate

Note:

metals, transition metals, metals with low melting point, molten salts, salts with low melting point, salts with melting point, metals with melting point

Note:

Strongly basic solutions employed as, for example, an antisolvent, may be, for example, buffered to a slightly lower pH to ensure the basic solution is compatible with, for example, the membranes and membrane-based processes that may be employed. For example, an aqueous solution of NaOH alone may have a pH as low as 1. A ‘buffered’ version of is solution may contain, for example, a less basic or an acidic compound, for example, sodium carbonate. A ‘buffered’ version of this solution may comprise, for example, a combination of sodium carbonate and sodium hydroxide or sodium carbonate alone, and may possess a pH of, for example 11-13.

Example and Experimental Data

Example reagent composition demonstrating precise UCST cloud point temperature and Cloud Point Temperature Adjustment or Tuning with Significant to Complete Reversibility At large Scale and Relatively Low Viscosity:

The below example compositions provide the exact cloud point temperature of a novel UCST system composition. The below compositions also demonstrate the relatively small adjustments in composition that may be employed to adjust the cloud point temperature or UCST of the liquid system. The below compositions also demonstrate the ability to adjust the size and composition of the bottom and top liquid layers formed from the UCST phase change. Some of the below compositions also demonstrate fully tunable UCST compositions comprising only non-toxic, non-volatile or nearly non-volatile chemicals (for example: water vapor). Some of the below compositions also demonstrate fully tunable UCST compositions comprising only non-corrosive or low corrosivity reagents. Some of the below compositions also demonstrate fully tunable UCST compositions comprising no or limited presence of an ionic compound.

It is important to note the one or more phases forming below the UCST temperature in a UCST system, one or more of the phases may have different density compared to one or more other phases. As a result, the one or more phases may form liquid ‘layers,’ where each layer is concentrated or comprises each liquid phase. The appearance of the liquid phases, may include, but is not limited to, the appearance of the liquid layers that form in a combination of mineral oil and DI water.

Note:

The presence of most ionic compounds comprising, for example, including, but not limited to, sodium chloride, potassium bicarbonate, potassium carbonate, ammonium bicarbonate, ammonium carbonate, ammonium phosphates, ammonium sulfate, increase the UCST cloud point temperature in aqueous systems with, for example, Polypropylene Glycol or Polyethylene Glycol. In aqueous systems with, for example, Polypropylene Glycol, the cloud point temperature increases with increased concentration of glycerol. In aqueous systems with, for example, Polypropylene Glycol, the cloud point temperature decreases with increased concentration of propylene glycol.

Example Composition #1 Composition 19.4 wt % PPG 425 53.6 wt % Propylene Carbonate 27 wt % Deionized Water Cloud Point Temperature ~18° C. Volume % of Top Layer ~45.5%   Below Cloud Point Temperature Composition of Top Layer Water + PPG 425 Rich Phase Volume % of Bottom Layer ~54.5%   Below Cloud Point Temperature Composition of Bottom Propylene Carbonate Rich Phase Layer Example Composition #2 Composition 23.0 wt % PPG 425 51.2 wt % Propylene Carbonate 25.8 wt % Deionized Water Cloud Point Temperature ~4.1° C. Volume % of Top Layer ~51% Below Cloud Point Temperature Composition of Top Layer Water + PPG 425 Rich Phase Volume % of Bottom Layer ~49% Below Cloud Point Temperature Composition of Bottom Propylene Carbonate Rich Phase Layer Example Composition #3 Composition 19.3 wt % PPG 425 48.4 wt % Propylene Carbonate 32.3 wt % Deionized Water Cloud Point Temperature ~18° C. Volume % of Top Layer ~57% Below Cloud Point Temperature Composition of Top Layer Water + PPG 425 Rich Phase Volume % of Bottom Layer ~43% Below Cloud Point Temperature Composition of Bottom Propylene Carbonate Rich Phase Layer Example Composition #4 Composition 21.5 wt % PPG 425 39.2 wt % Propylene Carbonate 39.3 wt % Deionized Water Cloud Point Temperature ~13.6° C. Volume % of Top Layer ~77% Below Cloud Point Temperature Composition of Top Layer Water + PPG 425 Rich Phase Volume % of Bottom Layer ~23% Below Cloud Point Temperature Composition of Bottom Propylene Carbonate Rich Phase Layer Example Composition #5 Composition 21.5 wt % PPG 425 39.0 wt % Propylene Carbonate 39.25 wt % Deionized Water 0.25 wt % Ammonium Sulfate Cloud Point Temperature ~15.6° C. Volume of Top Layer Below ~73.3%   Cloud Point Temperature Composition of Top Layer Water + PPG 425 + Ammonium Sulfate Rich Solution Volume of Bottom Layer ~26.7%   Below Cloud Point Temperature Composition of Bottom Propylene Carbonate - Rich Solution Layer

Composition #5 shows the presence of a relatively small concentration of ammonium sulfate (for example: 0.25 wt %) increases the UCST cloud point temperature of the liquid system relative to Composition #4.

Example Composition #6 Composition 21.2 wt % PPG 425 38.3 wt % Propylene Carbonate 38.6 wt % Deionized Water 1.9 wt % Glycerol Cloud Point Temperature ~17.3° C. Volume of Top Layer Below ~73.3% Cloud Point Temperature Composition of Top Layer Water + PPG 425 + Glycerol - Rich Solution Volume of Bottom Layer ~26.7% Below Cloud Point Temperature Composition of Bottom Propylene Carbonate - Rich Solution Layer

Composition #6 shows the presence of a relatively small concentration of glycerol (for example: 1.9 wt %) increases the UCST cloud point temperature of the liquid system relative to Composition #4.

Example Composition #7 Composition 21.1 wt % PPG 425 38.3 wt % Propylene Carbonate 38.5 wt % Deionized Water 2.2 wt % Propylene Glycol Cloud Point Temperature ~11.9° C. Volume of Top Layer Below ~84.5% Cloud Point Temperature Composition of Top Layer Water + PPG 425 + Propylene Glycol - Rich Solution Volume of Bottom Layer ~15.5% Below Cloud Point Temperature Composition of Bottom Propylene Carbonate - Rich Solution Layer

Composition #7 shows the presence of a relatively small concentration of propylene glycol (for example: 2.2 wt %) decreases the UCST cloud point temperature of the liquid system relative to Composition #4.

Example reagent composition demonstrating precise LCST cloud point temperature and Cloud Point Temperature Adjustment or Tuning with Significant to Complete Reversibility At Large Scale and Relatively Low Viscosity:

The below example compositions provide the exact cloud point temperature of a novel LCST system composition. The below compositions also demonstrate the relatively small adjustments in composition that may be employed to adjust the cloud point temperature or LCST of the liquid system. The below compositions also demonstrate the ability to adjust the size and composition of the bottom and top liquid layers formed from the LCST phase change. Some of the below compositions also demonstrate fully tunable LCST compositions comprising only non-toxic, non-volatile or nearly non-volatile chemicals (for example: water vapor). Some of the below compositions also demonstrate fully tunable LCST compositions comprising only non-corrosive or low corrosivity reagents. Some of the below compositions also demonstrate fully tunable LCST compositions comprising no or limited presence of an ionic compound.

It is important to note the one or more phases forming above the LCST temperature in a LCST system, one or more of the phases may have different density compared to one or more other phases. As a result, the one or more phases may form liquid ‘layers,’ where each layer is concentrated or comprises each liquid phase. The appearance of the liquid phases, may include, but is not limited to, the appearance of the liquid layers that form in a combination of mineral oil and DI water.

Note:

The presence of most ionic compounds comprising, for example, including, but not limited to, sodium chloride, potassium bicarbonate, potassium carbonate, ammonium bicarbonate, ammonium carbonate, ammonium phosphates, ammonium sulfate, decrease the LCST cloud point temperature in aqueous systems with, for example, Polypropylene Glycol or Polyethylene Glycol. In aqueous systems with, for example, Polypropylene Glycol, the cloud point temperature decreases with increased concentration of glycerol. In aqueous systems with, for example, Polypropylene Glycol, the cloud point temperature increases with increased concentration of propylene glycol.

Example Composition #8 Composition 32.8 wt % PPG 425 65.3 wt % Deionized Water 1.9 wt % Sodium Chloride Cloud Point Temperature ~35.9° C. Example Composition #9 Composition 32.3 wt % PPG 425 64.4 wt % Deionized Water 3.3 wt % Sodium Chloride Cloud Point Temperature ~28.2° C. Volume % of Top Layer ~23.2% Above Cloud Point Temperature Composition of Top Layer PPG 425 Rich Phase Volume % of Bottom Layer ~76.8% Above Cloud Point Temperature Composition of Bottom Water + Sodium Chloride Rich Phase Layer

Composition #9 shows increasing the concentration of sodium chloride decreases the cloud point temperature of the liquid system relative to Composition #8.

Example Composition #10 Composition 30.4 wt % PPG 425 60.5 wt % Deionized Water 6.0 wt % Polyethylene Glycol Dimethyl Ether (PEGDME) 250 3.1 wt % Sodium Chloride Cloud Point Temperature ~28.9° C. Volume % of Top Layer ~24.2% Above Cloud Point Temperature Composition of Top Layer PPG 425 + PEGDME 250 Rich Phase Volume % of Bottom Layer ~75.8% Above Cloud Point Temperature Composition of Bottom Water + Sodium Chloride Rich Phase Layer Example Composition #11 Composition 28.4 wt % PPG 425 56.7 wt % Deionized Water 12.0 wt % Polyethylene Glycol Dimethyl Ether (PEGDME) 250 2.9 wt % Sodium Chloride Cloud Point Temperature #1 ~29° C. Volume % of Top Layer ~17.0% Above Cloud Point Temperature (Cloud Point #1) Composition of Top Layer PPG 425 + PEGDME 250 Rich Phase Volume % of Bottom Layer ~83.0% Above Cloud Point Temperature (Cloud Point #1) Composition of Bottom Water + Sodium Chloride Rich Phase Layer Cloud Point Temperature #2 ~35° C. Volume % of Top Layer ~22.7% Above Cloud Point Temperature (Cloud Point #2) Composition of Top Layer PPG 425 + PEGDME 250 Rich Phase Volume % of Bottom Layer ~77.3% Above Cloud Point Temperature (Cloud Point #2) Composition of Bottom Water + Sodium Chloride Rich Phase Layer Example Composition #12 Composition 49.3 wt % PPG 425 49.3 wt % Deionized Water 1.4 wt % Sodium Chloride Cloud Point Temperature ~34.1° C. Volume % of Top Layer   ~60% Above Cloud Point Temperature Composition of Top Layer PPG 425 Rich Phase Volume % of Bottom Layer   ~40% Above Cloud Point Temperature Composition of Bottom Water + Sodium Chloride Rich Phase Layer Example Composition #13 Composition 20.0 wt % PPG 425 57.9 wt % Deionized Water 20.2 wt % Propylene Carbonate 1.8 wt % Ammonium Sulfate Cloud Point Temperature ~31.5° C. Volume % of Top Layer   ~65% Above Cloud Point Temperature Composition of Top Layer Water + Ammonium Sulfate Rich Phase Volume % of Bottom Layer   ~35% Above Cloud Point Temperature Composition of Bottom Propylene Carbonate + PPG-425 Layer Rich Phase

Example Composition #13 shows PPG 425+Propylene Carbonate+Water+Salt solutions may form a LCST system with or without a UCST with different relative concentrations of reagents than, for example, Composition #5.

Example UCST Phase Change Solution CO₂ Solubility Swing UCST Cloud Point ~28° C. Temperature Viscosity Top Layer ~2.1 cP Volume % of Top Layer ~59% Above Cloud Point Temperature Composition of Top Layer Organic-Lean CO2 Solubility at 30 PSI 5.21 g/kg solvent Gauge Pressure (46.696 PSI CO2 Partial Pressure) at 25° C. in Top Layer Viscosity of Bottom Layer ~3.7 cP Volume % of Bottom Layer ~41% Above Cloud Point Temperature Composition of Bottom Organic-Rich Layer CO2 Solubility at 30 PSI 16.88 g/kg solvent Gauge Pressure (46.696 PSI CO2 Partial Pressure) at 25° C. in Bottom Layer CO2 Solubility at 30 PSI 3.62 g/kg solvent Gauge Pressure (46.696 PSI CO2 Partial Pressure) at 30° C. in Combined Solution Example LCST Phase Change Solution CO₂ Solubility Swing UCST Cloud Point ~26° C. Temperature Viscosity of Top Layer ~4.7 cP Volume % of Top Layer ~52% Above Cloud Point Temperature Composition of Top Layer Organic-Rich CO2 Solubility at 30 PSI 17.14 g/kg solvent Gauge Pressure (46.696 PSI CO2 Partial Pressure) at 25° C. in Top Layer Viscosity of Bottom Layer ~1.6 cP Volume % of Bottom Layer ~48% Above Cloud Point Temperature Composition of Bottom Organic-Lean Layer CO2 Solubility at 30 PSI 4.51 g/kg solvent Gauge Pressure (46.696 PSI CO2 Partial Pressure) at 25° C. in Bottom Layer CO2 Solubility at 30 PSI 6.33 g/kg solvent Gauge Pressure (46.696 PSI CO2 Partial Pressure) at 20° C. in Combined Solution

Example Physical/Physio-Chemical Solvent:

The present solvent may be a physical solvent for acid gas removal with significant cost and performance improvements over competing physical solvents, such as Selexol. Composition #1 may comprise, for example, 20-99% (weight percent, wt %) solvent, including, but not limited to, water and 0.1-80 wt % of one or more or a combination of the following—phosphates of alkalis, alkaline earths, or ammonia, ammonium, which may further comprise dibasics or dihydrogens or di-cations of alkalis, alkaline earths, or ammonia, ammonium.

Highlights of Example:

-   -   Similar CO₂ solubility to Selexol     -   Solvent cost 20× less than Selexol.     -   Lower foaming than Selexol     -   Lower viscosity than Selexol     -   Non-volatile solvent     -   Lower methane loss than Selexol

Physical Solvent Technology Comparison Table Composition #1 (may comprise a concentrated solution of Diammonium Selexol Parameter Phosphate) (PEGDME 250) Water Scrubbing CO2 Solubility at 30 PSI 18.71 g/kg 19.36 g/kg 4.82 g/kg Gauge Pressure (46.696 solvent solvent1 solvent PSI CO2 Partial Pressure) at 25° C. Market Price of Solvent $141-$194 $29102 $0.3-2.00 (USD per metric ton) Methane Loss Likely <2% 1-4%** 0.5-2%** Viscosity at 25° C. (cP) <2 5.83 1 Process Pressure 4-7 bar (est.)* 4-7 bar** 5-10 bar** Proper Desulfurization No No** No** Chemicals Needed Yes Yes** No** Volatility Non-Volatile Non-Volatile Non-Volatile (exc. water vapor) *Composition #1 may be viable with total biogas absorption pressures below 4 bar (~2 bar CO₂ partial pressure). Larger solvent volumes or recirculation rates are generally required at lower CO₂ absorption pressures. Composition #1 may be viable under these lower pressure conditions because it has lower viscosity and significantly lower solvent cost than Selexol, while possessing similar CO₂ solubility.

Example Compositions, Temperatures, and Pressures

-   -   The UCST working fluids described herein may include         compositions that possess a UCST temperature that is adjustable         or tunable to any temperature from −20-1000° C.     -   The LCST working fluids introduced herein may include         compositions that possess a LCST temperature that is adjustable         or tunable to any temperature from −20*1000° C.     -   UCST reagent compositions include, but are not limited to, one         or more or a combination of the following: water, organic         solvent, polymer, glycol, carbonate, carbonate ester, ester,         ether, diol, lactam, protic solvents, aprotic solvents, amide,         alcohol, fluorinated compound, halogenated compound,         hydrocarbon, organic polymer, alkylene glycol, alkylene         carbonate, polyol, urea, ionic liquid, imine, amine, amide,         imide, azide, azine, acrylamide, acrylic, carboxylic acid,         ketone, aldehydes, alkaloids, halides, carbonyl, nitrile,         acetyl, peroxide, ionic compounds, epoxide, thioester, acetal,         alkane, alkene, alkyne, haloalkane, hydroperoxide, methoxy,         Carboxylate, cyanate, nirate, nitrite, nitroso, oximine,         carbamate, pyridine, organic sulfur compound, organic         phosphorous compound, boron, boron containing compound,         inorganic chemical, inorganic compound, enol     -   LCST reagent compositions include, but are not limited to, one         or more or a combination of the following: water, organic         solvent, polymer, glycol, carbonate, carbonate ester, ester,         ether, diol, lactam, protic solvents, aprotic solvents, amide,         alcohol, fluorinated compound, halogenated compound,         hydrocarbon, organic polymer, alkylene glycol, alkylene         carbonate, polyol, urea, ionic liquid, imine, amine, amide,         imide, azide, azine, acrylamide, acrylic, carboxylic acid,         ketone, aldehydes, alkaloids, halides, carbonyl, nitrile,         acetyl, peroxide, ionic compounds, epoxide, thioester, acetal,         alkane, alkene, alkyne, haloalkane, hydroperoxide, methoxy,         Carboxylate, cyanate, nirate, nitrite, nitroso, oximine,         carbamate, pyridine, organic sulfur compound, organic         phosphorous compound, boron, boron containing compound,         inorganic chemical, inorganic compound, enol     -   The solubility of one or more gases may be less than, equal to,         or greater than including, but not limited to, one or more of         the following: 0.00001 g per kg solvent, 0.01 g per kg solvent,         0.1 g per kg solvent, 0.5 g per kg solvent, 1 g per kg solvent,         1.5 g per kg of solvent, 2 g per kg of solvent, 3 g per kg of         solvent, 4 g per kg of solvent, 5 g per kg of solvent, 6 g per         kg of solvent, 7 g per kg of solvent, 8 g per kg of solvent, 9 g         per kg of solvent, 10 g per kg of solvent, 11 g per kg of         solvent, 12 g per kg of solvent, 13 g per kg of solvent, 14 g         per kg of solvent, 15 g per kg of solvent, 16 g per kg of         solvent, 17 g per kg of solvent, 18 g per kg of solvent, 19 g         per kg of solvent, 20 g per kg of solvent, 21 g per kg of         solvent, 22 g per kg of solvent, 23 g per kg of solvent, 24 g         per kg of solvent, 25 g per kg of solvent, 26 g per kg of         solvent, 27 g per kg of solvent, 28 g per kg of solvent, 29 g         per kg of solvent, 30 g per kg of solvent, 40 g per kg of         solvent, 50 g per kg of solvent, 60 g per kg of solvent, 70 g         per kg of solvent, 80 g per kg of solvent, 90 g per kg of         solvent, 100 g per kg of solvent, 110 g per kg of solvent, 150 g         per kg of solvent, 200 g per kg of solvent, 300 g per kg of         solvent, 400 g per kg of solvent, 500 g per kg of solvent, 750 g         per kg of solvent, 1000 g per kg of solvent, 1500 g per kg of         solvent, 2000 g per kg of solvent     -   Methane losses may be equal to, greater than, or less than one         or more or a combination of the following: 0.00001%, 0.0001%,         0.001%, 0.01%, 0.1%, 0.2%, 0.3%, 0.4%, 0.5%, 0.6%, 0.7%, 0.8%,         0.9%, 1.0%, 1.1%, 1.2%, 1.3%, 1.4%, 1.5%, 1.6%, 1.7%, 1.8%,         1.9%, 2.0%, 2.1%, 2.2%, 2.3%, 2.4%, 2.5%, 2.6%, 2.7%, 2.8%,         2.9%, 3.0%, 3.5%, 4.0%, 4.5%, 5%, 10%     -   Applications for the embodiments described herein, may include,         but are not limited to, one or more or a combination of the         following: acid gas removal, hydrocarbon-hydrocarbon separation,         hydrocarbon-inert gas separation, acid gas processing, natural         gas processing, gas processing, syngas purification, syngas acid         gas removal, CO₂ removal from steam methane reforming gases, CO₂         removal from steam biomass reforming gases biogas upgrading, CO₂         removal from hydrocarbon reforming gases, biogas upgrading, gas         treatment, CO₂ capture, post-combustion capture, pre-combustion         capture, landfill gas, flue gas, air separation, gas         concentrating, gas removal, aerosol removal, aerosol separation,         enhanced oil recovery with or without supercritical fluids,         enhanced oil recovery gas processing, enhanced oil recovery gas         processing for CO₂ reinjection, separation of Fischer-Tropsch         gases or liquids.     -   Reagents, compounds, ionic compounds, solvents, or substances         may include, but are not limited to, one or more or a         combination of the following: H−, H+, D−, D+, H2−, H2+, H3+,         He−, He+, He, H+, He2+, Li−, Li+, Na−, Na+, K−, K+, Cu−, Cu+,         LiH−, LiH+, NaH−, NaH+, KH+, Be−, Be+, Mg−, Mg+, Ca−, Ca+, Zn−,         Zn+, BeH−, BeH+, MgH−, MgH+, CaH+, ZnH+, BeH2+, B−, B+, Al−,         Al+, Sc+, Ga−, Ga+, BH−, BH+, AlH−, AlH+, ScH+, GaH+, BH2−,         BH2+, AlH2−, o2AlH2+, BH3−, BH3+, AlH3−, AlH3+, BH4−, AlH4−, C−,         C+, Si−, Si+, Ti−, Ti+, Ge−, Ge+, CH−, CH+, SiH−, SiH+, GeH+,         CH2−, CH2+, SiH2−, SiH2+, GeH2−, CH3−, CH3+, SiH3−, SiH3+,         GeH3+, CH4−, CH4+, SiH4+, N−, N+, P−, P+, V+, As−, As+, NH−,         NH+, PH−, PH+, AsH+, NH2−, NH2+, PH2−, PH2+, AsH2+, NH3−, NH3+,         PH3+, AsH3+, NH4+, PH4+, O−, O+, S−, S+, Se−, Se+, OH−, OH+,         HS−, HS+, CrH+, HSe−, HSe+, H2O−, H2O+, H2S−, H2S+, H2Se+, H3O+,         H3S+, H3Se+, F−, F+, Cl−, Cl+, Br−, Br+, I−, I+, HF−, HF+, HCl−,         HCl+, HBr−, HBr+, H2F+, H2Cl+, H2Br+, Ne−, Ne+, Ar−, Ar+, Kr+,         NeH+, ArH+, KrH+, XeH+, Li2−, Li2+, NaLi−, NaLi+, Na2−, Na2+,         NaK+, Be2−, Be2+, Mg2−, Mg2+, B2−, B2+, Al2−, Al2+, BC−, BC+,         C2−, C2+, SiC−, SiC+, Si2−, Si2+, C2H−, C2H+, C2H2+, H2CC−,         HCCH−, C2H3−, C2H3+, C2H4−, C2H4+, C2H5−, C2H5+, C2H6+, C2H7+,         LiN+, BeN−, BeN+, BN−, AlN−, AlN+, BN+, CN−, CN+, CP−, CP+,         SiN−, SiN+, SiP−, SiP+, N2−, N2+, PN−, PN+, P2−, P2+, HCN−,         HCN+, NNH+, HPO+, CNH2+, H2CN+, HCNH+, N2H2+, CH2NH2+, N2H4+,         CH3NH2+, N2H5+, CH3NH3+, CH3PH3+, LiO−, LiO+, LiS+, NaO−, NaO+,         KO+, BeO−, BeO+, MgO−, MgO+, MgS−, MgS+, BeS−, BeS+, BO−, AlO−,         AlO+, BS−, BS+, AlS−, AlS+, BO+, CO−, CO+, CS−, CS+, SiO−, SiO+,         SiS−, SiS+, CSe−, CSe+, GeO+, NO−, NO+, NS−, NS+, PO−, PO+, PS−,         PS+, O2−, O2+, SO−, SO+, S2−, S2+, SeO−, SeO+, SeS−, SeS+, Se2−,         Se2+, COH+, HCO−, HCO+, HCS−, HCS+, HNO−, HNO+, NOH+, HNS−,         HO2−, HO2+, KOH2+, H2CO−, H2CO+, H2CS−, H2CS+, H2O2+, H2S2+,         CH2OH+, CH3O−, CH3O+, H2CSH+, H3O2+, CH3OH−, CH3OH+, CH3SH+,         CH3OH2+, CH3SH2+, H5O2+, LiCl−, LiCl+, NaF−, NaF+, NaCl−, NaCl+,         LiBr−, LiBr+, NaBr−, NaBr+, LiF−, LiF+, BeF−, BeF+, MgF−, MgF+,         MgCl−, MgCl+, ZnF−, ZnF+, BeCl−, BeCl+, BF−, BF+, AlF−, AlF+,         BCl−, BCl+, AlCl−, AlCl+, GaF+, GaCl+, CF−, CF+, CCl−, CCl+,         SiF−, SiF+, SiCl−, SiCl+, GeF+, NF−, NF+, NCl−, NCl+, PF−, PF+,         PCl−, PCl+, FO−, FO+, ClO−, ClO+, SF−, SF+, SCl−, SCl+, BrO−,         F2−, F2+, ClF, ClF+, Cl2−, Cl2+, BrF−, BrF+, BrCl−, BrCl+, Br2−,         Br2+, 12+, HOBr+, F2H+, FHF−, Cl2H+, CH3C1H+, LiNe+, Ne2+, Ar2+,         Li3+, C3+, C3H3−, C3H3+, C3H3+, C3H5+, C3H7+, C3H7+, C3H7+, N3−,         N3+, CH3CN−, CH3CN+, HNCNH2+, NCNH3+, C2H5NH+, C2H6N+,         (CH3)2NH2+, CH3CH2NH3+, Li2O+, CNO−, NCO−, SCN−, BO2−, BO2+,         N2O−, N2O+, CO2−, CO2+, OCS+, CS2−, CS2+, NO2−, NO2+, PO2−,         PO2+, O3−, O3+, SO2−, SO2+, S3−, S3+, SeO2+, HCO2−, HNNO+,         NNOH+, HOCO+, HNO2+, O3H+, SO2H+, CH2CO+, H2COO+, CH3CO−,         CH3CO+, CH3OO−, CH3OO+, H2CONH2+, C2H4OH+, C2H4OH+, CH3CHOH+,         FCO+, CF2−, CF2+, SiF2+, CCl2−, CCl2+, ClOO+, OOO−, OClO+, NF2+,         SF2−, SF2+, F3−, Cl3−, HCCF+, HFCO+, CH2CHF+, C4+, C4H2+, C2N2+,         HCCCN+, C3H3N+, CH3NHN2+, CH6N3+, (CH3)3NH+, C3H7NH3+, CO3−−,         NO3−, NO3+, SO3−, SO3+, HCO3−, C2H2O2+, H2NO3+, CH3COO−, H3CO3+,         NH2CONH2+, NH2COOH2+, NH3COOH+, CH5N2O+, H2NCOHNH2+, CH3COCH3−,         CH3COHCH3+, C2Cl2+, BF3−, BF3+, ClO3−, CF3−, CF3+, SiF3+, CCl3−,         CCl3+, SiC13+, NF3−, NF3+, NF3H+, AsF3H+, CH2ClCH2OH2+, C5H5−,         C3H3N2−, C4H4N−, C4H6N+, C4H6N+, C4H6N+, NC4H12+, C302+, PO4−−−,         SO4−−, H5O4−, C4H4O+, C4HlOO+, ClO4−, BF4−, CCl4+, C2HF3+,         C6H5−, C6H6+, C6H7+, C5H6N+, C2O4−−, CF3CN+, C2F4+, SiF5−, SFS+,         C7H7+, CF3COO−, PF6−, C6N4−, H, H, D, D, H2, H2, H3, He, He, He,         H, He2, Li, Li, Na, Na, K, K, Cu, Cu, LiH, Li, NaH, NaH, KH, Be,         Be, Mg, Mg, Ca, Ca, Zn, Zn, BeH, BeH, MgH, MgH, CaH, ZnH, BeH2,         B, B, Al, Al, Sc, Ga, Ga, BH, BH, AlH, AlH, ScH, GaH, BH2, BH2,         AlH2, o2AlH2, BH3, BH3, AlH3, AlH3, BH4, AlH4, C, C, Si, Si, Ti,         Ti, Ge, Ge, CH, CH, SiH, SiH, GeH, CH2, CH2, SiH2, SiH2, GeH2,         CH3, CH3, SiH3, SiH3, GeH3, CH4, CH4, SiH4, N, N, P, P, V, As,         As, NH, NH, PH, PH, AsH, NH2, NH2, PH2, PH2, AsH2+, NH3, NH3,         PH3, AsH3, NH4, PH4, O, O, S, S, Se, Se, OH, OH, HS, HS, CrH,         HSe, HSe, H2O, H2O, H2S, H2S, H2Se, H3O, H3S, H3Se, F, F, Cl,         Cl, Br, Br, I, I, HF, HF, HCl, HCl, HBr, HBr, H2F, H2C1, H2Br,         Ne, Ne, Ar, Ar, Kr, NeH, ArH, KrH, XeH, Li2, Li2, NaLi, NaLi,         Na2, Na2, NaK, Be2, Be2, Mg2, Mg2, B2, B2, Al2, Al2, BC, BC, C2,         C2, SiC, SiC, Si2, Si2, C2H, C2H, C2H2, H2CC, HCCH, C2H3, C2H3,         C2H4, C2H4, C2H5, C2H5, C2H6, C2H7, LiN, BeN, BeN, BN, AlN, AlN,         BN, CN, CN, CP, CP, SiN, SiN, SiP, SiP, N2, N2, PN, PN, P2, P2,         HC, HCN, NNH, HPO, CNH2, H2CN, HCNH, N2H2, CH2NH2, N2H4, CH3NH2,         N2H5, CH3NH3, CH3PH3, LiO, LiO, LiS, NaO, NaO, KO, BeO, BeO,         MgO, MgO, MgS, MgS, BeS, BeS, BO, Al, AlO, BS, BS, AlS, AlS, BO,         CO, CO, CS, CS, SiO, SiO, SiS, SiS, CSe, CSe, GeO, NO, NO, NS,         NS, PO, PO, PS, PS, O2, O2, SO, SO, S2, S2, SeO, SeO, SeS, SeS,         Se2, Se2, COH, HCO, HCO, HCS, HCS, HNO, HNO, NOH, HNS, HO2, HO2,         KOH2, H2CO, H2CO, H2CS, H2CS, H2O2, H2S2, CH2OH, CH3O, CH3O,         H2CSH, H302, CH3OH, CH3OH, CH3 SH, CH3OH2, CH3SH2, H5O2, LiCl,         LiCl, NaF, NaF, NaCl, NaCl, LiBr, LiBr, NaBr, NaBr, LiF, LiF,         BeF, BeF, MgF, MgF, MgCl, MgCl, ZnF, ZnF, BeCl, BeCl, BF, BF,         AlF, AlF, BCl, BCl, AlCl, AlCl, GaF, GaCl, CF, CF, CCl, CCl,         SiF, SiF, SiCl, SiCl, GeF, NF, NF, NO, NO, PF, P, PCI, PC, FO,         FO, ClO, ClO, SF, SF, SCI, SCI, BrO, F2, F2, ClF, ClF, Cl2, Cl2,         BrF, BrF, BrCl, BrCl, Br2, Br2, I2, HOBr, F2H, FHF−, Cl2H,         CH3ClH, LiNe, Ne2, Ar2, Li3, C3, C3H3, C3H3, C3H3, C3H5, C3H7,         C3H7, C3H7, N3, N3, CH3CN, CH3CN, HNCNH2, NCNH3, C2H5NH, C2H6N,         (CH3)2NH2, CH3CH2NH3, Li2O, CNO, NCO, SCN, BO2, BO2, N2O, N2O,         CO2, CO2, OCS, CS2, CS2, NO2, NO2, PO2, PO2, O3, O3, SO2, SO2,         S3, S3, SeO2, HCO2, HNNO, NNOH, HOCO, HNO2, O3H, SO2H, CH2CO,         H2COO, CH3CO, CH3CO, CH3OO, CH3OO, H2CONH2, C2H4OH, C2H4OH,         CH3CHOH, FCO, CF2, CF2, SiF2, CCl2, CCl2, ClOO, OClO, OClO, NF2,         SF2, SF2, F3, Cl3, HCCF, HFCO, CH2CHF, C4, C4H2, C2N2, HCCCN,         C3H3N, CH3NHN2, CH6N3, (CH3)3NH, C3H7NH3, CO3, NO3, NO3, SO3,         SO3, HCO3, C2H2O2, H2NO3, CH3COO, H3CO3, NH2CONH2, NH2COOH2,         NH3COOH, CH5N2O, H2NCOHNH2, CH3COCH3, CH3COHCH3, C2Cl2, BF3,         BF3, ClO3, CF3, CF3, SiF3, CCl3, CCl3, SiC13, NF3, NF3, NF3H,         AsF3H, CH2ClCH2OH2, C5H5, C3H3N2, C4H4N, C4H6N, C4H6N, C4H6N,         NC4H12, C3O2, PO4, SO4, HSO4, C4H4O, C4HlOO, ClO4, BF4, CCl4,         C2HF3, C6H5, C6H6, C6H7, C5H6N, C2O4, CF3CN, C2F4, SiF5, SF5,         C7H7, CF3COO, PF6, C6N4, ionic liquids     -   Physical solvents, including thermally switchable solubility         solvents, include, but are not limited to, one or more or a         combination of the following: PEGDMEs, PPGs, PEGs, polymers,         organic solvents, Ethylene carbonate, propylene carbonate,         glycol ethers, water, ionic liquids,     -   Reagents include, but are not limited to, PEGDMEs, PPGs, PEGs,         polymers, organic solvents, Ethylene carbonate, propylene         carbonate, glycol ethers, water, ionic liquids,         Dimethoxymethane, Diethoxymethane, Diethoxyethane, Diethyl         Ether, Dimethyl Ether     -   Cloud Point Temperatures heating or LCST temperature or         combination thereof may include, but are not limited to, equal         to, greater than, or less than one or more or a combination of         the following: −100° C., or −90° C., or −80° C., or −70° C., or         −60° C., or −50° C., or −40° C., or −30° C., or −20° C., or −10°         C., 0° C., 1° C., 2° C., 3° C., 4° C., 5° C., 6° C., 7° C., 8°         C., 9° C., 10° C., 11° C., 12° C., 13° C., 14° C., 15° C., 16°         C., 17° C., 18° C., 19° C., 20° C., 21° C., 30° C., 40° C., 50°         C., 60° C., 70° C., 80° C., 90° C., 100° C., 110° C., 120° C.,         130° C., 140° C., 150° C., 140° C., 150° C., 200° C., 500° C.,         1000° C., 2000° C., 3000° C., 10000° C., 100000° C.     -   Cloud Point Temperatures cooling or UCST temperature or         combination thereof may include, but are not limited to, equal         to, greater than, or less than one or more or a combination of         the following: −100° C., or −90° C., or −80° C., or −70° C., or         −60° C., or −50° C., or −40° C., or −30° C., or −20° C., or −10°         C., 0° C., 1° C., 2° C., 3° C., 4° C., 5° C., 6° C., 7° C., 8°         C., 9° C., 10° C., 11° C., 12° C., 13° C., 14° C., 15° C., 16°         C., 17° C., 18° C., 19° C., 20° C., 21° C., 30° C., 40° C., 50°         C., 60° C., 70° C., 80° C., 90° C., 100° C., 110° C., 120° C.,         130° C., 140° C., 150° C., 140° C., 150° C., 200° C., 500° C.,         1000° C., 2000° C., 3000° C., 10000° C., 100000° C.     -   Absorption unit operations may include, but are not limited to,         one or more or a combination of the following: absorption         column, column, contactor, gas-liquid contactor, liquid-liquid         contactor, liquid solid contactor, membrane contactor, gas         membrane contactor, packed column, membrane column, plated         column, multistage column, solid handling column, liquid         handling column, multiphase column, rotating absorption unit,         kinetic motion absorption unit, stripping column, mixing vessel,         continuously stirred reactor, pressurization vessel,         depressurization vessel, multistage vessel, batch setup, mixing         of two or more phases, formation of more phases from less         phases, formation of less phases from relatively more phases,         heating vessel, cooling vessel, membrane absorption, membrane         selective absorption     -   Desorption unit operations may include, but are not limited to,         one or more or a combination of the following: column,         contactor, gas-liquid contactor, membrane column, membrane         contactor, gas membrane contactor, packed column, plated column,         multistage column, multistage vessel, batch setup, liquid-liquid         contactor, liquid solid contactor, solid handling column, liquid         handling column, multiphase column, rotating desorption unit,         kinetic motion desorption unit, stripping column, mixing vessel,         continuously stirred reactor, reboiler, depressurization vessel,         pressurization vessel, flash vessel, flash unit, multistage         flash unit, mixing of two or more phases, formation of more         phases from less phases, formation of less phases from         relatively more phases, heating vessel, cooling vessel, carrier         gas stripping, steam stripping, air stripping, recirculating gas         stripping, stripping using one or more gases being desorbed,         ammonia stripping, membrane stripping, membrane distillation,         membrane selective absorption     -   Acid Gases, include, but are not limited to, one or more or a         combination of the following applications: acid gas removal,         hydrocarbon-hydrocarbon separation, hydrocarbon-inert gas         separation, acid gas processing, natural gas processing, gas         processing, gas plants for purification and/or re-injection of         CO₂, H₂S, or other acid gases into oil field, syngas         purification, syngas acid gas removal, CO₂ removal from steam         methane reforming gases, CO₂ removal from steam biomass         reforming gases biogas upgrading, CO₂ removal from hydrocarbon         reforming gases, biogas upgrading, gas treatment, CO₂ capture,         post-combustion capture, pre-combustion capture, landfill gas,         flue gas,     -   CO₂, or other acid gas or gases, Partial Pressure Shifting         Reagents may include, but are not limited to, one or more or a         combination of the following:         -   Acidic Reagents, or solubility or concentration or pH             changing acidic reagents including, but are not limited to,             one or more or a combination of the following: boric acid,             an acidic reagent with pKa less acidic than the anion bonded             to the reagent cation, an acidic reagent comprising an             acidic salt, ammonium nitrate, ammonium sulfate, ammonium             chloride, monoammonium phosphate, monosodium phosphate, one             or more phosphate salts,         -   CO₂ solubility reducing compounds, including, but not             limited to, one or more or a combination of the following:             aqueous solutions, water, salts with salting out properties,             salts with significant solubility swing, compounds with             significant solubility swing, salts with significant             solubility swing with temperature, urea, thermally             switchable reagents,     -   Hydrocarbons, may include, but are not limited to, one or more         or a combination of the following: compound containing carbon,         compound containing hydrogen, compound containing oxygen,         compound containing nitrogen, compound containing sulfur,         saturated hydrocarbon, unsaturated hydrocarbon, cyclic         hydrocarbon, cyclo hydrocarbon, aromatic hydrocarbon, alkane,         alkene, alkyne, cycloalkane, alkadiene, polymers, halogenated         hydrocarbons, hydrocarbons with one or more functional groups,         one or more hydrocarbons in crude oil, one or more different         hydrocarbons in crude oil, one or more hydrocarbons in naphtha,         one or more hydrocarbons in gasoline, one or more hydrocarbons         in diesel, one or more hydrocarbons in heavy oil, one or more         hydrocarbons in natural gas, natural gas liquids, one or more         hydrocarbons in kerosene, organic solvents, light hydrocarbons,         heavy hydrocarbons, water insoluble hydrocarbons, partially         water soluble hydrocarbons, water soluble hydrocarbons, low         toxicity hydrocarbons, medium toxicity hydrocarbons, high         toxicity hydrocarbons, methane, Ethane, Ethene (ethylene),         Ethyne (acetylene), Propane, Propene (propylene), Propyne         (methylacetylene), Cyclopropane, Propadiene, Butane, Butene         (butylene), Butyne, Cyclobutane, Butadiene, Pentane, Pentene,         Pentyne, Cyclopentane, Pentadiene, (piperylene), Hexane, Hexene,         Hexyne, Cyclohexane, Hexadiene, Heptane, Heptene, Heptyne,         Cycloheptane, Heptadiene, Octane, Octene, Octyne, Cyclooctane,         Octadiene, hydrocarbon solution, hydrocarbon containing mixture     -   Superior properties for desorption may include, but are not         limited to, one or more or a combination of the following:         higher equilibrium partial pressure of one or more gases or         different gases, lower equilibrium partial pressure of one or         more gases or different gases, faster desorption kinetics,         greater desorption of a desired gas relative to a less desired         gas, low viscosity, low volatility of other solvent         constituents, low relative volatility of other solvent         constituents, no degradation, no corrosion, minimal degradation,         minimal corrosion, compatibility with gas impurities, minimal         impurities in desorbed gases     -   Salts may include, but are not limited to, one or more or a         combination of the following: ionic compounds, ionic liquids,         anions, cations, complex salts, complex ions, compounds with         properties similar to salts, salts with properties dissimilar to         salts, alkali, alkaline-earth, transition metal, metal,         semiconductor, metalloids, ammonia, ammonium, amine, basic         compound, halogenated compound, sulfate, nitrate, carbonate,         hydrogen carbonate, carbamate, nitrite, sulfite, carbon         compound, sulfur compound, electrolyte, nitrogen compound,         phosphorous compound, phosphorous containing anion, halogen         containing anion     -   Gas, Liquid, aqueous, solid, dissolved, one or more ionic         species or forms, one or more liquid phase species, biphasic         mixture, multiphasic mixture, multiphasic mixture comprising         liquids, solid mixture, supercritical, hydrate, triple-point, or         combination thereof.     -   Carbon Dioxide (gas), Carbon Dioxide (liquid), Carbon Dioxide         (aqueous), Carbon Dioxide (solid), Carbon Dioxide (dissolved),         Carbon Dioxide (one or more ionic species), Carbon Dioxide (one         or more liquid phase species), Carbon Dioxide (solid mixture),         Carbon Dioxide (supercritical), Carbon Dioxide (Hydrate), Carbon         Dioxide (triple point), Acidic Substance (gas), Acidic Substance         (liquid), Acid Substance (aqueous), Acidic Substance Gas         (Hydrate) Acidic Substance (solid), Acidic Substance         (dissolved), Acidic Substance (one or more ionic species),         Acidic Substance (one or more liquid phase species), Acidic         Substance (solid mixture), Acid Substance (supercritical),         Acidic Substance (triple point), Basic Compound (gas), Basic         Compound (liquid), Basic Compound (solid), Basic Compound         (dissolved), Basic Compound (one or more ionic species), Basic         Compound (one or more liquid phase specific), Basic Compound         (solid mixture), Basic Compound (supercritical), Basic Compound         (hydrate), Basic Compound (triple point), Hydrocarbon (gas),         Hydrocarbon (liquid), Hydrocarbon (aqueous), Hydrocarbon         (dissolved), Hydrocarbon (non-aqueous), Hydrocarbon (one or more         ionic species), Hydrocarbon (one or more liquid phase species),         Hydrocarbon (solid), Hydrocarbon (solid mixture), Hydrocarbon         (supercritical), Hydrocarbon (Hydrate), Hydrocarbon (triple         point).     -   Viscosity is greater than, equal to, or less than 100,000 cP, or         10,000 cP, or 1,000 cP, or 500 cP, or 100 cP, or 50 cP, or 40         cP, or 30 cP, or 20 cP, or 10 cP, or 9 cP, or 8 cP, or 7 cP, or         6 cP, or 5 cP, or 4 cP, or 3 cP, or 2 cP, or 1 cP or 0.5 cP, or         combination thereof     -   Cooling Inputs or Sources include, but are not limited to, one         or more or a combination of the following: thermocline water         body, thermocline liquid body, water body, cold liquid body,         evaporative cooling, heat pump cooling, air cooling, heat         exchange with enthalpy source, cyrogenic cooling, LNG         gasification, pressure reduction, cold surface, radiative         cooling, endothothermic phase change     -   Heating Inputs or Sources include, but are not limited to, one         or more or a combination of the following: Waste Heat, Ambient         Temperature Changes, Diurnal Temperature Variation, Thermocline         liquid body, thermocline solid body, thermocline gaseous body,         Thermocline of a water body, halocline, heat pump, solar         thermal, solar thermal pond, light, electricity, steam,         combustion, compression, pressure increase, geothermal,         radiative heat, condensation, exothermic dissolution, exothermic         precipitation, exothermic formation of more liquid phases,         exothermic formation of less liquid phases, exothermic phase         change, or other heat sources described herein.     -   Temperatures: temperatures of operation are greater than, less         than, or equal to or a combination thereof include, but are not         limited to, one or more or a combination of the following: −100°         C., or −90° C., or −80° C., or −70° C., or −60° C., or −50° C.,         or −40° C., or −30° C., or −20° C., or −10° C., 0° C., 1° C., 2°         C., 3° C., 4° C., 5° C., 6° C., 7° C., 8° C., 9° C., 10° C., 11°         C., 12° C., 13° C., 14° C., 15° C., 16° C., 17° C., 18° C., 19°         C., 20° C., 21° C., 30° C., 40° C., 50° C., 60° C., 70° C., 80°         C., 90° C., 100° C., 110° C., 120° C., 130° C., 140° C., 150°         C., 140° C., 150° C., 200° C., 500° C., 1000° C., 2000° C.,         3000° C., 10000° C., 100000° C.     -   Mass percentages of one or more components comprise greater than         or less than or equal to one or more or a combination of the         following: 0.0000001%, 0.001%, 0.01%, 0.1%, 1%, or 5%, or 10%,         or 11%, or 12%, or 13%, or 14%, 15%, or 16%, or 17%, or 18%, or         19%, or 20%, or 21%, or 22%, or 23%, or 24%, or 25%, or 26%, or         27%, or 28%, or 29%, or 30%, or 31%, or 32%, or 33%, or 34%, or         35%, or 36%, or 37%, or 38%, or 39%, or 40%, or 41%, or 42%, or         43%, or 44%, or 45%, or 46%, or 47%, or 48%, or 49%, or 50%, or         51%, or 52%, or 53%, or 54%, or 55%, or 56%, or 57%, or 58%, or         59%, or 60%, or 65%, or 70%, or 75%, or 80%, or 85%, or 90%, or         95%, or less than or equal to 100%.     -   Relative mass distribution of one or more liquid phases may         include, but is not limited to, greater than or less than or         equal to one or more or a combination of the following:         0.0000001%, 0.001%, 0.01%, 0.1%, 1%, or 5%, or 10%, or 11%, or         12%, or 13%, or 14%, 15%, or 16%, or 17%, or 18%, or 19%, or         20%, or 21%, or 22%, or 23%, or 24%, or 25%, or 26%, or 27%, or         28%, or 29%, or 30%, or 31%, or 32%, or 33%, or 34%, or 35%, or         36%, or 37%, or 38%, or 39%, or 40%, or 41%, or 42%, or 43%, or         44%, or 45%, or 46%, or 47%, or 48%, or 49%, or 50%, or 51%, or         52%, or 53%, or 54%, or 55%, or 56%, or 57%, or 58%, or 59%, or         60%, or 65%, or 70%, or 75%, or 80%, or 85%, or 90%, or 95%, or         less than or equal to 100%.     -   A ‘substantial’ concentration of one or more components (For         Example: substances or reagents or solvents or antisolvents) may         include, but is not limited to, mass percentages of one or more         components comprising greater than or equal to one or more or a         combination of the following: 1%, or 5%, or 10%, or 11%, or 12%,         or 13%, or 14%, 15%, or 16%, or 17%, or 18%, or 19%, or 20%, or         21%, or 22%, or 23%, or 24%, or 25%, or 26%, or 27%, or 28%, or         29%, or 30%, or 31%, or 32%, or 33%, or 34%, or 35%, or 36%, or         3′7%, or 38%, or 39%, or 40%, or 41%, or 42%, or 43%, or 44%, or         45%, or 46%, or 4′7%, or 48%, or 49%, or 50%, or 51%, or 52%, or         53%, or 54%, or 55%, or 56%, or 57%, or 58%, or 59%, or 60%, or         65%, or 70%, or 75%, or 80%, or 85%, or 90%, or 95%, or less         than or equal to 100%.     -   pH may be greater than or equal to or less than one or more or a         combination of the following: 1, or 2, or 3, or 4, or 5, or 6,         or 7, or 8, or 9, or 10, or 11, or 12, or 13, or 14     -   Separation Devices may include, but are not limited to, one or         more or a combination of the following: decanter, separatory         funnel, coalescer, centrifuge, filter, switchable solvent,         cyclone, semi-permeable membrane, nanofiltration, organic         solvent nanofiltration, reverse osmosis, ultrafiltration,         microfiltration, hot nanofiltration, hot ultrafiltration,         distillation, membrane distillation, flash distillation,         multi-effect distillation, mechanical vapor compression         distillation, or hybrid systems     -   (a) Membrane—Based Separation comprising one or a combination of         the following:         -   a. Nanofiltration         -   b. Organic Solvent Nanofiltration         -   c. Reverse Osmosis         -   d. Forward Osmosis         -   e. Ultrafiltration         -   f. Microfiltration     -   (b) Distillation comprising one or a combination of the         following:         -   a. Batch distillation         -   b. Continuous distillation         -   c. Simple distillation         -   d. Fractional distillation         -   e. Steam distillation         -   f. Azeotropic distillation         -   g. Multi-effect distillation         -   h. Multi-stage flash distillation         -   i. Flash distillation         -   j. Mechanical vapor compression distillation         -   k. Membrane distillation         -   l. Vacuum distillation         -   m. Short path distillation         -   n. Zone distillation         -   o. Air sensitive distillation     -   (c) Switchable solvent—one or a combination of the following:         -   a. Thermally switchable         -   b. CO₂-switchable         -   c. Switchable solvents responsive to other changes to system             conditions.

comprise water, organic solvent, siloxanes, ionic liquids, water soluble polymer, soluble polymer, glycol, polyethylene glycol, polypropylene glycol, ethers, glycol ethers, glycol ether esters, triglyme, polyethylene glycols of multiple geometries, including, branched polyethylene glycols, star polyethylene glycols, comb polyethylene glycols, methoxypolyethylene glycol, polyvinyl alcohol, polyvinylpyrrolidone, polyacrylic Acid, diol polymers, 1,2 propanediol, 1,2 ethanediol, 1,3 propanediol, cellulose ethers, methylcellulose, cellosize, carboxymethylcellulose, hydroxyethylcellulose, sugar alcohol, sugars, alcohols, ketones, aldehydes, esters, organosilicon compounds, halogenated solvents, non-volatile solvents, a substance with a vapor pressure less than 0.01 atm at 20° C., soluble substances with a molecular weight greater than 80 daltons, volatile organic solvents, soluble substances with a molecular weight less than 600 daltons, soluble substances with a molecular weight less than 200 daltons, dimethoxymethane, acetone, acetaldehyde, methanol, dimethyl ether, THF, ethanol, isopropanol, propanal, methyl formate, azeotropes, alcohols, ketones, aldehydes, esters, organosilicon compounds, halogenated solvents, a substance with a vapor pressure greater than than 0.01 atm at 20° C., or a mixture thereof.

water, ammonia, ammonium, amine, azine, amino ethyl ethanol amine, 2-amino-2-methylpropan-1-ol (AMP), MDEA, MEA, primary amine, secondary amine, tertiary amine, low molecular weight primary or secondary amine, metal-ammine complex, metal-ammonia complex, metal-ammonium complex, sterically hindered amine, imines, azines, piperazine, alkali metal, lithium, sodium, potassium, rubidium, caesium, alkaline earth metal, calcium, magnesium, ionic liquid, thermally switchable compounds, CO₂ switchable compounds, enzymes, metal-organic frameworks, quaternary ammonium, quaternary ammonium cations, quaternary ammonium cations embedded in polymer, or mixtures thereof

ion exchange, ion exchange membrane, electrodialysis, or removal or replacement of the absorbent and/or CO₂ containing solution.

Convenient sources from which to capture CO₂ for the CO₂ containing solution include sources selected from the group consisting of flue gas; combustion emissions; manufacturing emissions; refining emissions or a combination thereof. Such sources may include, for example, from combustion of one or more hydrocarbons; emissions from the combustion of natural gas, coal, oil, petcoke, gasoline, diesel, biofuel, or municipal waste; emissions from waste water treatment gases, or landfill gases, from air, from metal production/refining, from the production of Iron, Steel, Aluminum or Zinc, from cement production, from quicklime production, from Glass production, oil and gas refineries, steam reforming, hydrogen production, HVAC, refrigeration, transportation vehicles (ships, boats, cars, buses, trains, trucks, airplanes), natural gas, biogas, alcohol fermentation, volcanic activity, decomposing leaves/biomass, septic tank, respiration, manufacturing facilities, fertilizer production, geothermal wells, and combinations thereof.

The amounts of gas to be captured or concentrated or removed from one or more sources will vary. Typically, it is desired to capture at least about any of the following percentages (%) from the total CO₂ in the source: 40, or 50, or 60, or 70, or 80, or 90, or substantially 100.

The one or more gases may be captured from any convenient source using any convenient manner. If desired, the input gas stream or streams may be treated, e.g., scrubbed, before being subjected to the one or more absorption solutions and/or forming a gas-rich, such as CO₂-rich, solution. Such treating methods may be particularly advantageous if the source has impurities that may deleteriously affect subsequent processing steps. Such impurities include, but are not limited to, NOx, SOx, oils, particulate matter, heavy metals, and heavy compounds, etc. Conventional treating methods may be employed for this purpose.

The amounts of CO₂ to be desorbed will vary. Typically, it is desired to desorb at least about any of the following percentages (%) from the total CO₂ in the source: 40, or 50, or 60, or 70, or 80, or 90, or substantially 100%.

The soluble substance employed may vary depending upon, for example, whether it is to be at least partially recovered, and, if so, in what manner. By “at least partially recovered” it is meant from at least about 50%, or at least about 60%, or at least about 70%, or at least about 80%, or at least about 90%, or at least about 95%, or at least about 99% up to 100% of the soluble solvent is recovered for re-use in the process or something else.

For example, the separation mechanism used for at least partially recovering the soluble substance may include one or more or a combination of the following: membrane, reverse osmosis, hot reverse osmosis, nanofiltration, organic solvent nanofiltration, hot nanofiltration, ultrafiltration, hot ultrafiltration, microfiltration, filtration, distillation, membrane distillation, multi-effect distillation, mechanical vapor compression distillation, binary distillation, azeotrope distillation, hybrid separation devices, flash distillation, multistage flash distillation, extractive distillation, switchable solvent, LCST phase change, UCST phase change, ‘salting-out,’ or centrifuge, or combinations thereof.

The soluble substance may be at least partially recovered by employing a membrane that is, for example, capable of at least partially rejecting said soluble substance while allowing substantial passage of CO₂ or containing aqueous solution or vice versa. “CO₂ containing solution” or “CO₂ containing aqueous solution” simply refers to the subsequently obtained solution after desorbing of CO₂. Thus, CO₂ containing aqueous solution or CO₂ containing solution may have various amounts of CO₂ or even no CO₂ depending upon the amount of CO₂ desorbed in the desorbing step. This subsequently obtained solution typically comprises the solution components less any CO₂ desorbed while any soluble substance is at least partially recovered by virtue of being rejected by the membrane.

Soluble substance may comprise, for example, water, organic solvent, water soluble polymer, soluble polymer, glycol, polyethylene glycol, polypropylene glycol, ethers, glycol ethers, glycol ether esters, triglyme, polyethylene glycols of multiple geometries, including, branched polyethylene glycols, star polyethylene glycols, comb polyethylene glycols, methoxypolyethylene glycol, polyvinyl alcohol, polyvinylpyrrolidone, polyacrylic Acid, diol polymers, 1,2 propanediol, 1,2 ethanediol, 1,3 propanediol, cellulose ethers, methylcellulose, cellosize, carboxymethylcellulose, hydroxyethylcellulose, sugar alcohol, sugars, alcohols, ketones, aldehydes, esters, organosilicon compounds, halogenated solvents, non-volatile solvents, a substance with a vapor pressure less than 0.01 atm at 20° C., soluble substances with a molecular weight greater than 80 daltons, or mixtures thereof.

Useful membranes for at least partial recovery may include, for example, any membrane capable of at least partially rejecting said soluble substance while allowing substantial passage of CO₂ containing solution or gas containing solution or vice versa. Such membranes may comprise a membrane selected from the group consisting of Reverse Osmosis, Nanofiltration, Organic Solvent Nanofiltration, Ultrafiltration, Microfiltration, and Filtration membranes. In some embodiments the membrane may have a molecular weight cutoff of greater than about 80 daltons. That is, the membrane allows passage of a substantial or majority amount of components with a molecular weight of less than about 80 daltons while rejecting a substantial or majority amount of components with a molecular weight of greater than about 80 daltons up to about 600 daltons. In the art, another definition of molecular weight cut-off may refer to the lowest molecular weight solute (in daltons) in which 90% of the solute is retained by the membrane, or the molecular weight of the molecule that is 90% retained by the membrane. Membranes with a molecular weight cutoff of less than 1,000 daltons, or less than 10,000 daltons, or less than 50,000 daltons, or less than 100,000 daltons, or less than 200,000 daltons, or less than 500,000 daltons, or less than 1,000,000 daltons may also be useful depending upon the circumstances and components employed.

The membrane may be comprised of any useful material and such useful material may vary depending upon the components to be separated, their molecular weight, viscosity, and/or other properties. Useful membranes may include, for example, membranes comprised of a material selected from a thin film composite; a polyamide; a cellulose acetate; a ceramic membrane; other materials and combinations thereof.

Generally, it may be preferred to select membranes, substances, and conditions such that any at least partial recovery step(s) involving one or more membranes may be conducted at a temperature of less than or equal to about 50, or less than or equal to 40, or less than or equal to about 35, or less than or equal to about 30° C. In other specific embodiments the at least partial recovery step(s) temperature may be at a temperature of from about 18° C. to about 32° C. Similarly, the pressure employed during any at least partial recovery may be any convenient pressure, e.g., elevated, reduced, or substantially atmospheric.

One or more substances may comprise, for example, one or more or a combination of the following: volatile organic solvents, soluble substances with a molecular weight less than 600 daltons, soluble substances with a molecular weight less than 200 daltons, dimethoxymethane, acetone, acetaldehyde, methanol, dimethyl ether, THF, ethanol, isopropanol, propanal, methyl formate, azeotropes, alcohols, ketones, aldehydes, esters, organosilicon compounds, halogenated solvents, a substance with a vapor pressure greater than than 0.01 atm at 20° C., or a mixture thereof.

The integrated process wherein CO₂ volatilizes may occur in the presence of a low CO₂ partial pressure gas, in the presence of air, with the application of heat, or a combination thereof.

In some embodiments the soluble substance may comprise a thermally switchable substance, a CO₂ switchable substance, or a non-ionic carbon containing compound. A switchable substance is one which substantially separates from other materials depending upon, for example, a property or other ingredients of a combined composition. That is, a thermally switchable substance may form one or more separate liquid phases or precipitate from a given solution or a combination thereof when subjected to temperatures above or below a certain threshold, e.g., cloud point.

The concentration of the soluble substance(s) and any CO₂ absorbent employed in the integrated process may vary depending upon the substance, other substances, and desired results. Typically, each may have a concentration of from about 1M to about 18M. That is, the concentration of each may be independent or dependent of the other and be, for example, greater

The concentration of the soluble substance(s) and any CO₂ absorbent employed in the integrated process may vary depending upon the substance, other substances, and desired results. Typically, each may have a concentration of from about 1M to about 18M. That is, the concentration of each may be independent or dependent of the other and be, for example, greater or less than 1M, or less than 2M, or less than 3M, or less than 4M, or less than 5M, or less than 6M or less than 10M up to as high as 18M.

The absorption column may absorb less than or equal to any of the following: 5%, or 10% or 20%, or 30%, or 40%, or 50%, or 60%, or 70%, or 80% or 90%, or 99%, or 99.9%, or 100% of one or more gases from the one or more gas streams.

The absorption stage may include any absorption setup known in the art and may be composed of one or more absorption columns or vessels or other devices. The absorption column may include, but is not limited to, continuous absorption, continuous stirred absorption, batch column, packed column, plate column, hybrid absorption processes and other absorption processes known in the art. The absorption column or absorption solution may be chilled, wherein cooling may be conducted via any means including, but not limited to, ambient source, water bodies, cooling tower, industrial evaporative chiller and other chilling or cooling processes known in the art. It may be desirable for the CO₂ concentration in the CO₂ lean solution to be less than the CO₂ concentration in the CO₂ rich solution. A CO₂(g) containing gas stream, including but not limited to flue gas, synthesis gas, steam-reforming gas, methane reforming gas, hydrogen production gases, air, concentrated, membrane concentrated gas stream, membrane concentrated flue gas, upstaged air (as would be created from the moisture swing CO₂ upstaging processes described by Klaus Lackner http://pubs.acs.org/doi/abs/10.1021/es201180v, incorporated herein by reference), biogas, landfill gas, or anaerobic digester gas. The CO₂ containing gas stream may be treated, used as an enthalpy, heat or cold source, or otherwise used prior to the absorption stage.

The remaining gas stream after at least a portion of CO₂(g) or other gas is absorbed, or ‘inert gases’ may undergo further treatment or utilization, including but not limited to, thermal or other exchange with incoming CO₂ lean solution, water wash to remove trace gases, such as ammonia or organic solvent, removal process for trace gases, additional CO₂ scrubbing method, including, but not limited to, amines, solid sorbent, SELEXOL, UCARSOL, membrane or strong base, separation, purification, or use of constituents, such as hydrogen, carbon monoxide, nitrogen, oxygen and/or argon.

water, ammonia, ammonium amine, primary amine, secondary amine, tertiary amine, methylamine (MEA), methylethanolamine, aminoethylethanolamine, azine, imine, strong base, hydroxide, sodium hydroxide, potassium hydroxide, sodium oxide, potassium oxide, organic solvent, commercial CO₂ capture absorbents, quaternary ammonium compound, Selexol, Rectisol, KS-1, UCARSOL, metal-organic framework, solid adsorbent, high surface area compounds, activated carbon, zeolites, carbon nanotubes, graphene, graphene oxide, amine, amino ethyl ethanol amine, 2-Amino-2-methylpropan-1-ol (AMP), MDEA, MEA, primary amine, secondary amine, or tertiary amine, low molecular weight primary or secondary amine, metal-ammine complex, metal-ammonia complex, metal-ammonium complex, sterically hindered amine, imines, azines, piperazine, amine functionalized polymers, alkali metal, lithium, sodium, potassium, rubidium, caesium, alkaline earth metal, calcium, magnesium, cations, ionic liquid, CO₂ switchable solvents, CO₂ switchable surfactants carbonate, polymer containing amine functional groups, poler containing CO₂ reactive functional groups, enzymes, metal-organic frameworks, glycolamine, diglycolamine, quaternary ammonia or quaternary ammonium cations, or quaternary ammonium cations embedded in polymer, or mixtures thereof.

piperazine, diethanolamine, diglycolamine, and diisopropanolamine

residence time, added substance type or types, soluble substance concentration in the mixed CO₂ desorption solution, concentration of the soluble substance in the added substance solution, temperature, application of heating or cooling, CO₂ loading in the CO₂ rich solution, pressure, or CO₂ loading in the in the added substance solution.

Small concentrations of soluble substance may persist or be present in the CO₂ absorption solution. Low concentrations of soluble substances, such as organic solvents, may reduce ammonia slip or other CO₂ absorbent volatilization in the absorption column and reduce energy consumption during regeneration. Additionally, low concentrations of soluble substances, such as organic solvents, may increase CO₂ uptake and inhibit unintended CO₂ volatilization. The maximum said low concentration is dependent on the type of substance and includes, but is not limited to, vol/vol % concentrations of less than any of the following: 0.001%, or 0.1%, or 0.5%, or 1%, or 1.5%, or 2%, or 2.5%, or 3%, or 3.5%, or 4%, or 4.5%, or 5%, or 5.5%, or 6%, or 6.5%, or 7%, or 7.5%, or 8%, or 8.5%, or 9%, or 9.5%, or 10%, or 10.5%, or 11%, or 11.5%, or 12%, or 12.5%, or 13%, or 13.5%, or 14%, or 14.5%, or 15%, or 20%, or 30%, or 40%, or 50%, or 60%, or 70%, or 80%, or 90%, or 100%.

Carbon Dioxide Sources: Any process or resource producing or containing carbon dioxide. Examples of CO₂ sources include, but are not limited to, the following: Power Plant (Natural gas, coal, oil, petcoke, biofuel, municipal waste), Waste Water Treatment, Landfill gas, Air, Metal production/refining (such as Iron, Steel, Aluminum, etc.), Glass production, Oil refineries, HVAC, Transportation vehicles (ships, boats, cars, buses, trains, trucks, airplanes), Natural Gas, Biogas, Alcohol fermentation, Volcanic Activity, Decomposing leaves/biomass, Septic tank, Respiration, Manufacturing facilities, Fertilizer production, or Geothermal processes where CO₂(g) releases from a well or wells.

One or more embodiments may be aqueous or non-aqueous. Media include, for example, polar organic solvents, including, but not limited to, ethylene carbonate, propylene carbonate, ethylene glycol, propylene glycol, DMSO, water and acetonitrile or inorganic solvents, such as liquid ammonia or liquid amines and mixtures thereof. The non-aqueous system may use a solution media containing of one or more CO₂ absorbents, such as ammonia, ammonium, amines or amine functionalized polymers.

concentration may be as a low as 0.000001 M or as great as pure absorbent. In molarity terms, the concentration of the CO₂ absorbent may be as low as 0.00001M or less than any of the following: 0.01 M, or 0.05M, or 0.1M, or 0.3M, or 0.5M, or 0.8 M, or 1M, or 1.3M, or 1.5M, or 1.8M, or 2M, or 2.3M, or 2.5M, or 2.8M, or 3M, or 3.3M, or 3.5M, or 3.8M, or 4M, or 5M, or 6M, or 7M, or 8M, or 9M, or 10M, or 12M, or 15M, or 18M, or even pure absorbent.

concentration may be as a low as 0.000001 M or as great as pure absorbent. In molarity terms, the concentration of the CO₂ absorbent may be as low as 0.00001M or less than any of the following: 0.01 M, or 0.05M, or 0.1M, or 0.3M, or 0.5M, or 0.8 M, or 1M, or 1.3M, or 1.5M, or 1.8M, or 2M, or 2.3M, or 2.5M, or 2.8M, or 3M, or 3.3M, or 3.5M, or 3.8M, or 4M, or 5M, or 6M, or 7M, or 8M, or 9M, or 10M, or 12M, or 15M, or 18M, or even pure liquid phase.

concentration may be as a low as 0.000001 M or as great as pure absorbent. In molarity terms, the concentration of the CO₂ absorbent may be as low as 0.00001M or less than any of the following: 0.01 M, or 0.05M, or 0.1M, or 0.3M, or 0.5M, or 0.8 M, or 1M, or 1.3M, or 1.5M, or 1.8M, or 2M, or 2.3M, or 2.5M, or 2.8M, or 3M, or 3.3M, or 3.5M, or 3.8M, or 4M, or 5M, or 6M, or 7M, or 8M, or 9M, or 10M, or 12M, or 15M, or 18M, or even pure reagent.

concentration may be as a low as 0.000001 M or as great as pure absorbent. In molarity terms, the concentration of the CO₂ absorbent may be as low as 0.00001M or less than any of the following: 0.01 M, or 0.05M, or 0.1M, or 0.3M, or 0.5M, or 0.8 M, or 1M, or 1.3M, or 1.5M, or 1.8M, or 2M, or 2.3M, or 2.5M, or 2.8M, or 3M, or 3.3M, or 3.5M, or 3.8M, or 4M, or 5M, or 6M, or 7M, or 8M, or 9M, or 10M, or 12M, or 15M, or 18M, or even pure antisolvent.

The soluble substance may be preheated or cooled before injection into the mixing apparatus. The mixing apparatuses and methods include, but are not limited to, batch mixers, continuous stirred-tank reactors, CSTRs, distillation column, packed column, electrospray, spray column, countercurrent spray column, and/or other apparatuses and/or methods. The apparatus may be heated using waste heat or other heat source for, including, but not limited to, promoting gas desorption, promoting gas desorption, reducing viscosity and/or increasing the rate of solvent mixing.

The one or more gases, such as CO₂, may pressurize, by any means, including but not limited to, closing and opening a release valve to allow the system to pressurize, utilizing a smaller gas release valve, temperature change, or using external compression. In the case where the CO₂(g) is desorbed at a pressure greater than atmospheric pressure, less energy may be required for compression of this CO₂(g), if compression is desired. The exiting gas stream may contain predominantly CO₂. At least a portion of this desorbed CO₂ may be used for, including, but not limited to, one or more or a combination of the following: enhanced oil recovery, methanol production, syngas production, fuel production, urea production, fertilizer production, carbonate, bicarbonate production, carbamate production, beverage production, greenhouse, agricultural applications, welding gas, turbine working fluid, laser gas, food production, inert gas, cement production, CO₂ conversion processes, and other existing and future applications. This gas stream may be further treated by, including, but not limited to, water wash down, aqueous wash down, non-aqueous wash down, changes in pressure, changes in temperature, compression, vacuum, and an additional carbon capture process. Additives may be added to this gas stream prior, during or after treatment or in the absence of treatment. These additives include, but are not limited to, ammonia, electricity, light, hydrogen, amine, oxygen, methane, methanol, carbon monoxide, hydrogen sulfide, haloalkanes, chlormethane, dimethylether, hydrogen cyanide, sulfur, acid or acid gas, hydroxide, oxide, carbonate, carbamate, and bicarbonate.

Reagents or substances may include, but is not limited to, one or more or a combination of the following: organic solvents, concentrated soluble substance solutions, water soluble polymers, combinations of soluble substances, solvent mixtures, emulsions, pure substance, pure solvent, aqueous solvent, surfactant containing solvents, zwitterions, solids, soluble solids, gases, liquid-solid mixtures, soluble gases, aerosols, suspended solids, solid-gas mixtures, super critical fluids, and fluid mixtures.

Application of Heating or Cooling: Heating or cooling may be incorporated throughout the integrated process.

In water, Polyethylene glycols (PEGs) and polypropylene glycols (PPGs), for example, have higher Gibbs free energy of mixing and osmotic pressure at lower temperatures.

Concentrated solution of the soluble substance, including, but not limited to, physical solvent, antisolvent, combined solution, one or more liquid phases, concentrate, permeate, or combination thereof may contain a vol/vol % concentration of soluble substance as low as 0.0001% to as great as 99.99999%. Vol/vol % concentrations of the soluble substance or concentrated soluble substance solution may be practically greater than any of the following: 1%, or 5%, or 10%, or 11%, or 12%, or 13%, or 14%, 15%, or 16%, or 17%, or 18%, or 19%, or 20%, or 21%, or 22%, or 23%, or 24%, or 25%, or 26%, or 27%, or 28%, or 29%, or 30%, or 31%, or 32%, or 33%, or 34%, or 35%, or 36%, or 37%, or 38%, or 39%, or 40%, or 41%, or 42%, or 43%, or 44%, or 45%, or 46%, or 47%, or 48%, or 49%, or 50%, or 51%, or 52%, or 53%, or 54%, or 55%, or 56%, or 57%, or 58%, or 59%, or 60%, or 65%, or 70%, or 75%, or 80%, or 85%, or 90%, or 95%, or less than or equal to 100%.

The resulting concentration of the soluble substance in one or more gas desorption may be a mass % concentration of soluble substance as low as 0.0001% to as great as 99.99999%. Mass % concentrations of the soluble substance in the one or more desorption steps, absorption steps, or resulting mixed solution may be practically greater than any of the following: 0.0001, 0.1%, or 1%, or 2%, or 3%, or 4%, or 5%, or 5.5%, or 6%, or 6.5%, or 7%, or 7.5%, or 8%, or 8.5%, or 9%, or 9.5%, or 10%, or 10.5%, or 11%, or 11.5%, or 12%, or 12.5%, or 13%, or 13.5%, or 14%, or 14.5%, or 15%, or 15.5%, or 16%, or 16.5%, or 17%, or 17.5% or 18%, or 18.5%, or 19%, or 19.5%, or 20%, or 20.5%, or 21%, or 21.5%, or 22%, or 22.5%, or 23%, or 23.5% or 24%, or 24.5%, or 25%, or 25.5%, or 26%, or 26.5%, or 27%, or 27.5%, or 28%, or 28.5%, or 29%, or 29.5%, or 30%, or 31%, or 32%, or 33%, or 34%, or 35%, or 36%, or 37%, or 38%, or 39%, or 40%, or 41%, or 42%, or 43%, or 44%, or 45%, or 46%, or 47%, or 48%, or 49%, or 50%, or 51%, or 52%, or 53%, or 54%, or 55%, or 56%, or 57%, or 58%, or 59%, or 60%, or 65%, or 70%, or 75%, or 80%, or 85%, or 90%, or 95%, or less than 99%, or less than 100% or 100%.

Mass % solubility of one or more substances may be practically greater than any of the following: insoluble, 0.001%, 0.01%, 0.1%, or 1%, or 2%, or 3%, or 4%, or 5%, or 6%, or 7%, or 8%, or 9%, or 10%, or 11%, or 12%, or 13%, or 14%, or 15%, or 16%, or 17%, or 18%, or 19%, or 20%, or 21%, or 22%, or 23%, or 24%, or 25%, or 26%, or 27%, or 28%, or 29%, or 30%, or 31%, or 32%, or 33%, or 34%, or 35%, or 36%, or 37%, or 38%, or 39%, or 40%, or 41%, or 42%, or 43%, or 44%, or 45%, or 46%, or 47%, or 48%, or 49%, or 50%, or 51%, or 52%, or 53%, or 54%, or 55%, or 56%, or 57%, or 58%, or 59%, or 60%, or 61%, or 62%, or 63%, or 64%, or 65%, or 66%, or 67%, or 68%, or 69%, or 70%, or 71%, or 72%, or 73%, or 74%, or 75%, or 76%, or 77%, or 78%, or 79%, or 80%, or 81%, or 82%, or 83%, or 84%, or 85%, or 86%, or 87%, or 88%, or 89%, or 90%, or 90.5%, or 91%, or 91.5%, or 92%, or 92.5%, or 93%, or 93.5%, or 94%, or 94.5%, or 95%, or 95.5%, or 96%, or 96.5%, or 97%, or 97.5%, or 98%, or 98.5%, or 99%, or 99.5%, or 99.9%, or 100%, or completely miscible.

The desorbed gas concentration range may be as low as 0.0001% to as great as 99.99999%. The purity or concentration of the desorbed gas may be as low as any of the following: 0.1% or greater than 0.1%, or 1%, or 2%, or 3%, or 4%, or 5%, or 6%, or 7%, or 8%, or 9%, or 10%, or 11%, or 12%, or 13%, or 14%, or 15%, or 16%, or 17%, or 18%, or 19%, or 20%, or 21%, or 22%, or 23%, or 24%, or 25%, or 26%, or 27%, or 28%, or 29%, or 30%, or 31%, or 32%, or 33%, or 34%, or 35%, or 36%, or 37%, or 38%, or 39%, or 40%, or 41%, or 42%, or 43%, or 44%, or 45%, or 46%, or 47%, or 48%, or 49%, or 50%, or 51%, or 52%, or 53%, or 54%, or 55%, or 56%, or 57%, or 58%, or 59%, or 60%, or 61%, or 62%, or 63%, or 64%, or 65%, or 66%, or 67%, or 68%, or 69%, or 70%, or 71%, or 72%, or 73%, or 74%, or 75%, or 76%, or 77%, or 78%, or 79%, or 80%, or 81%, or 82%, or 83%, or 84%, or 85%, or 86%, or 87%, or 88%, or 89%, or 90%, or 90.5%, or 91%, or 91.5%, or 92%, or 92.5%, or 93%, or 93.5%, or 94%, or 94.5%, or 95%, or 95.5%, or 96%, or 96.5%, or 97%, or 97.5%, or 98%, or 98.5%, or 99%, or 99.5%, or 99.9%, or less than or equal to 100%.

Liquid CO₂, supercritical CO₂, or solid CO₂

The gas partial pressure range may be as low as 0.001 atm to as great as 100,000 atm. The partial pressure of one or more gases may be as low as, including, but not limited to, any of the following: 0.00001 atm, or 0.01 atm, or greater than or less than 0.05 atm, or 0.1 atm, or 0.2 atm, or 0.3 atm, or 0.4 atm, or 0.5 atm or 0.6 atm, or 0.7 atm, or 0.8 atm, or 0.9 atm, or 1 atm, or 1.1 atm, or 1.2 atm, or 1.3 atm, or 1.4 atm, or 1.5 atm, or 1.6 atm, or 1.7 atm, or 1.8 atm, or 1.9 atm, or 2 atm, or 2.1 atm, or 2.2 atm, or 2.3 atm, or 2.4 atm, or 2.5 atm, or 2.6 atm, or 2.7 atm, or 2.8 atm, or 2.9 atm, or 3 atm, or 3.5 atm, or 4 atm, or 4.5 atm, or 5 atm, or 5.5 atm, or 6 atm, or 6.5 atm, or 7 atm, or 7.5 atm, or 8 atm, or 8.5 atm, or 9 atm, or 9.5 atm, or 10 atm, or 12 atm, or 15 atm, or 18 atm, or 20 atm, or 22 atm, or 25 atm, or 28 atm, or 30 atm, or 40 atm, or 50 atm, or 60 atm, or 75 atm, or 100 atm, or 150 atm, or 200 atm, or 500 atm, or 1,000 atm, or 10,000 atm, or 100,000 atm, or less than 1,000,000 atm.

The purity or concentration of the desorbed gas or gases or final gas or gases produced may be dependent on the application. The setup may contain other gases than said desorbed gas or gases. The other gas or gases present in with this desorbed gas or gases may be dependent on the application. For example, if the CO₂ will be mixed with hydrogen (such as at about a 2:1 or 3:1 ratio) to produce CO₂ derived chemicals, hydrogen may be added as a headspace gas during CO₂ desorption. This example may reduce CO₂ capture energy requirements, including, but not limited to, due to the requirement of a lower partial pressure of CO₂(g) desorbed and lower final solvent concentration required.

System conditions may include, but are not limited to, one or more or a combination of the following: temperature, pressure, light, sound, vibration, radiation, electromagnetic radiation, magnetism, acid gas concentration, basic gas concentration, dissolved gas concentration, presence one or more other reagents, lack of presence of one or more reagents, change in reagent concentration, the presence of one or more stimulants, the lack of presence or reduced presence of one or more stimulants Separation devices and mechanisms include, but are not limited to, one or more or a combination of the following: coalescer, switchable solvent, cyclone, semi-permeable membrane, nanofiltration, organic solvent nanofiltration, reverse osmosis, ultrafiltration, microfiltration, hot nanofiltration, hot ultrafiltration, distillation, membrane distillation, flash distillation, multi-effect distillation, mechanical vapor compression distillation, hybrid systems, thermally switchable solvent, centrifuge, or filter or combinations thereof.

The power source of one or more pumps may include, but is not limited to, one or more or a combination of the following: electricity, pressure exchanger, turbocharger, hydraulic pressure, heat, pressure retarded osmosis, or forward osmosis.

Following the membrane or filter based separation, energy can be recovered by both or either the permeate (the absorption solution) and the concentrate (the soluble substance containing solution). These energy recovery devices are known in the art and include, but are not limited to, pressure exchangers and turbochargers.

Any portion of the process may be heated or cooled. Heat sources may include, but are not limited to, waste heat, power plant waste heat, steam, heat, pump or compressor waste heat, industrial process waste heat, steel waste heat, metal refining and production waste heat, paper mill waste heat, cement production waste heat, calcination waste heat, factory waste heat, petroleum refining waste heat, solar heat, solar pond, air conditioner waste heat, combustion heat, geothermal heat, ocean or water body thermal heat, stored heat, and CO₂(g) absorption solution heat. Temperatures of heating or cooling for any of the embodiments disclosed include, but are not limited to, less than any of the following: −20° C., or −10° C., or 0° C., or 10° C., or 20° C., or 25° C., or 30° C., or 35° C., or 40° C., or 41.5° C., or 41.5° C., or 41.5° C.-60° C., or 45° C., or 50° C., or 55° C., or 60° C., or 60-100° C., or 110° C., or 150° C.

Relatively lower molecular weight solvents may be employed if advantageous, including, but not limited to, polyethylene glycols 150-2000, polypropylene glycols 425-4000 and glycol ethers, such as triglyme.

1) exhibit lower viscosity, 2) higher solubility, 3) less prone to degradation, 4) less expensive, 5) lower concentration polarization, 6) higher mole fraction per given vol/vol %, 7) greater Gibbs free energy of mixing and 8) greater influence on dielectric constant,

9) lower osmotic pressure, 10) greater reduction of osmotic pressure with heat, 11) allow for the use of a larger pore size membrane or filter, 12) allow for the use of a higher permeability membrane, 13) may possess an LCST or UCST phase change with temperature or 14) may decrease in solubility with changes in temperature.

One or more embodiments may be constructed and transported in smaller scale modules or as a unit, such as in shipping containers and transported and used in other locations.

capture carbon dioxide in remote locations, in applications including, but not limited to, oil and gas production, cement production, mining and air CO₂ capture. One or more embodiments may also be constructed as stationary unit or units

One or more embodiments may employ a reverse osmosis membrane with a low molecular weight cut-off, including but not limited to, less than any of the following: 250 da, or 200 da, or 150 da, or 125 da, or 100 da, or 95 da, or 90 da, or 85 da, or 80 da, or 75 da

Multicomponent separation devices or multistage separation devices may be employed. Said device or devices may include, but are not limited to, one or more or a combination of the following: binary distillation, azeotrope distillation, membrane distillation, mechanical vapor compression, hybrid systems, flash distillation, multistage flash distillation, multieffect distillation, extractive distillation, switchable solvent, reverse osmosis, nanofiltration, organic solvent nanofiltration, ultrafiltration, and microfiltration. For example, such a hybrid system may involve at least partially recovering the soluble substance using nanofiltration and then further concentrating the soluble substance using membrane distillation. Another example of such a hybrid system may be a process wherein a switchable solvent ‘switches’ out of solution due to the presence of a stimulant, such as a change in temperature, then nanofiltration is employed to further concentrate the switchable solvent or remove remaining switchable solvent in other solution. The switchable solvent or other substance dissolved in solution may be further recovered or concentrated or even removed from the one or more layers or separate solutions that are formed.

Applied Pressure or Osmotic Pressure of Solution: The osmotic pressure range of the resulting water soluble substance solution may be as low as 0.001 atm to as great as 1,000,000 atm. The osmotic pressure may be as low as less than any of the following: 0.001 atm, or 0.01 atm, or greater than or less than 0.05 atm, or 0.1 atm, or 0.2 atm, or 0.3 atm, or 0.4 atm, or 0.5 atm or 0.6 atm, or 0.7 atm, or 0.8 atm, or 0.9 atm, or 1 atm, or 1.1 atm, or 1.2 atm, or 1.3 atm, or 1.4 atm, or 1.5 atm, or 1.6 atm, or 1.7 atm, or 1.8 atm, or 1.9 atm, or 2 atm, or 2.1 atm, or 2.2 atm, or 2.3 atm, or 2.4 atm, or 2.5 atm, or 2.6 atm, or 2.7 atm, or 2.8 atm, or 2.9 atm, or 3 atm, or 3.5 atm, or 4 atm, or 4.5 atm, or 5 atm, or 5.5 atm, or 6 atm, or 6.5 atm, or 7 atm, or 7.5 atm, or 8 atm, or 8.5 atm, or 9 atm, or 9.5 atm, or 10 atm, or 12 atm, or 15 atm, or 18 atm, or 20 atm, or 22 atm, or 25 atm, or 28 atm, or 30 atm, or 35 atm, or 40 atm, or 45 atm, or 50 atm, or 55 atm, or 60 atm, or 65 atm, or 70 atm, or 75 atm, or 80 atm, or 85 atm, or 90 atm, or 95 atm, or 100 atm, or 150 atm, or 200 atm, or 500 atm, or 1,000 atm, or 10,000 atm, or 100,000 atm, or less than 1,000,000 atm, or pure solvent.

Using waste heat or chilling to accelerate or foster gas desorption and other hybrid waste heat and membrane recovery process combinations

Solid precipitation and dissolution may occur throughout the process, including, but not limited to, due to changes in concentrations, concentrations, dissolved gas concentrations, pressures, temperature, other system conditions, or combinations thereof.

The particular mechanism used to separate one or more solutions may include, but is not limited to, one or more or a combination of the following: binary distillation, azeotrope distillation, mechanical vapor compression, membrane distillation, hybrid systems, flash distillation, multi stage flash distillation, multieffect distillation, extractive distillation, switchable solvent, reverse osmosis, nanofiltration, organic solvent nanofiltration, ultrafiltration, and microfiltration

one or more separation techniques, including, but not limited to, one or more or a combination of the following: filtration, centrifuge, decanting, distillation, magnetism, and/or membrane based process, such as reverse osmosis, osmotically assisted reverse osmosis, disc tube reverse osmosis (DTRO), high pressure reverse osmosis, forward osmosis, electrodialysis, nanofiltration, organic solvent nanofiltration ultrafiltration, membrane distillation, integrated electric-field nanofiltration, hot nanofiltration, or hot ultrafiltration

random or sequential copolymers of low molecular weight diols such as 1,2 propanediol, 1,2 ethanediol, and/or 1,3 propanediol.

Thermally responsive compounds include, but are not limited to, Lower Critical Solution Temperature (LCST) and Upper Critical Solution Temperature (UCST) compounds, thermosensitive magnetic nanoparticles, thermally responsive polyelectrolytes and thermally responsive ionic liquids.

LCST compounds are soluble or have a higher solubility below a certain threshold temperature, the lower critical solution temperature. For example, thermosensitive poly(N isopropylacrylamide) (PNIPAM) hydrogels can absorb water below the volume phase transition temperature (VPTT, ˜32C) and expel water at temperatures above the VPTT. Other examples of these hydrogel substances include polyacrylamide (PAM), PNIPAM, and poly(Nisopropylacrylamide-co-acrylic acid) and sodium (P(NIPAM-co-SA)). Non-hydrogel LCST compounds include, but are not limited to, Methylcellulose and triethylamine.

Examples of thermosensitive magnetic nanoparticles include, but are not limited to those described in the following article http://pubs.rsc.org/en/content/articlelanding/2011/cc/c1cc13944d#!divAbstract which is incorporated herein by reference. These nanoparticles are typically hydrophilic and are coated with various functional groups to allow them to generate osmotic pressure in solution.

Substances showing magnetic field based change in solubility or other form of recovery via changes in magnetic field may be useful. These include, but are not limited to, magnetic nanoparticles with added functional groups (such as those described in http://pubs.acs.org/doi/abs/10.1021/ie100438x, incorporated herein by reference), and magnetic or inductive heating of nanoparticles in solution.

Substances that change solubility or other recovery method due to pressure or a combination of pressure and temperature may also be useful. These include, but are not limited to, PSA, polyacrylamide (PAM), PNIPAM, and poly(Nisopropylacrylamide-co-acrylic acid sodium (P(NIPAM-co-SA)) hydrogels.

Changes in solution kinetic energy can act as a stimulus to change or promote a change in the solubility or other form of recovery of an added substance. Kinetic energy can be of various forms, including, but not limited to, mixing and sonication. Ultrasonic sonication may either increase or decrease solubility and to promote precipitation and crystal nucleation. Ultrasonic sonication may be used to increase the rate of CO₂ desorption.

a soluble substance, a water soluble substance, an organic solvent, an organic substance, a soluble organic substance, a water soluble organic solvent, a soluble polymer, a water soluble organic substance, a substance containing carbon, a substance containing carbon and hydrogen, a substance containing carbon, hydrogen and oxygen, or a substance containing hydrogen and nitrogen, a non-ionic substance, a non-reactive substance, a non-ionic water soluble substance, non-reactive water soluble substance, inert soluble substance, inert water soluble substance, or inert substance.

Switchable Hydrophilicity (SHS), Switchable Polarity (SPS), Switchable Water (SW).

Examples of waste heat sources include, but are not limited to, the following: Power Plant (Natural gas, coal, oil, petcoke, biofuel, municipal waste), Condensing water, Flue Gas, Steam, Oil refineries, Metal production/refining (Iron, Steel, Aluminum, etc.), Glass production, Manufacturing facilities, Fertilizer production, Transportation vehicles (ships, boats, cars, buses, trains, trucks, airplanes), Waste Water Treatment, Solar thermal, Solar pond, Solar photovoltaic, Geothermal (Deep Well), Biofuel powered vehicles, Biofuel/Biomass/Municipal Waste Power Plants, Desulfurization, Alcohol production, hydrogen sulfide treatment, acid (e.g. sulfuric) production, Renewable fertilizer production, Ocean Thermal, Space heating, Grey water, Diurnal temperature variation, Geothermal (Shallow well/loop), or respiration.

Heat or cooling may be applied at any point of one or more embodiments

Heat exchangers and recovery devices may be employed where advantageous.

nitrogen, oxygen, hydrogen, argon, methane, carbon monoxide, volatile hydrocarbons, such as ethane, butane, propane.

-   -   Mixing devices, include, but are not limited to, on or more or a         combination of the following:         -   CSTR, Batch, Semibatch, or flash devices         -   Turbine             -   Rushton Turbine             -   Smith Turbine             -   Helical Turbine             -   Bakker Turbine         -   Low shear mixer, High shear mixer, Dynamic mixer, Inline             mixer, Static mixer, Turbulent flow mixer, No mixer,             Close-clearance mixer, High shear disperser, Static mixers,             Liquid whistles, Mix-Itometer, Impeller mixer, Liquid-Liquid             mixing, Liquid-Solid mixing, Liquid-Gas mixing,             Liquid-Gas-Solid mixing, Multiphase mixing, Radial Flow,             Axial Flow, Flat or curved blade geometry

Any portion of the process may be heated or cooled. Heat sources may include, but are not limited to, waste heat, power plant waste heat, steam, heat, pump or compressor waste heat, industrial process waste heat, steel waste heat, metal refining and production waste heat, paper mill waste heat, factory waste heat, petroleum refining waste heat, solar heat, solar pond, air conditioner waste heat, combustion heat, geothermal heat, ocean or water body thermal heat, stored heat, and CO₂(g) absorption solution heat.

may comprise, including, but not limited to, one or more or a combination of the following phases throughout the integrated process: liquid, solid, liquid-solid slurry, liquid-solid mixture, gas, two-phase solution, three-phase solution, two-layer solution, or supercritical

Aqueous solution, Water soluble polymer, Soluble polymer, Glycol Polyethylene Glycol, Polypropylene Glycol Ethers, Glycol Ethers, Glycol ether esters, Triglyme. Polyethylene Glycols of multiple geometries, Methoxypolyethylene Glycol, Polyvinyl Alcohol Polyvinylpyrrolidone, Polyacrylic Acid, Diol polymers, 1,2 propanediol, 1,2 ethanediol, 1,3 propanediol, Cellulose Ethers, Methylcellulose, Cellosize, Carboxymethylcellulose, Hydroxyethylcellulose, Sugar Alcohol, Sugars, Alcohols Ketones, Aldehydes, Esters, Organosilicon compounds, Halogenated solvents

Non-Volatile Substances:

-   -   Poly(ethylene glycol) (PEG) and Poly(ethylene oxide) (PEO)         -   Heterobifunctional PEGs             -   Azide (—N3) Functionalized             -   Biotin Functionalized             -   Maleimide Functionalized             -   NHS Ester Functionalized             -   Thiol Functionalized             -   COOH Functionalized             -   Amine Functionalized             -   Hydroxyl Functionalized             -   Acrylate/Methacrylate Functionalized         -   Homobifunctional PEGs         -   Monofunctional PEGs         -   PEG Dendrimers and Multi-arm PEGs             -   PEG-core Dendrimers             -   Multi-arm PEGs             -   Multi-arm PEG Block Copolymers         -   PEG Copolymers             -   PEG Diblock Copolymers             -   PEG/PPG Triblock Copolymers             -   Biodegradable PEG Triblock Copolymers             -   Multi-arm PEG Block Copolymers             -   Random Copolymers         -   PEG and Oligo Ethylene Glycol             -   Examples: PEG 200, PEG 300, PEG 400, PEG 600, PEG 1000,                 PEG 1450, PEG 1500, PEG 2050, PEG 3350, PEG 8000, PEG                 10000         -   Poly(ethylene oxide)         -   High Oligomer Purity PEG         -   Polyethylene glycol-polyvinyl alcohol (PEG-PVA)     -   Polypropylene Glycol (PPG)         -   Examples: PPG 425-4000     -   Poly(N-isopropylacrylamide) (PNIPAM) and Polyacrylamide (PAM)         -   PNIPAM Copolymers         -   Poly(N-isopropylacrylamide) (PNIPAM)         -   Polyacrylamide (PAM) and Copolymers     -   Poly(2-oxazoline) and Polyethylenimine (PEI)     -   Poly(acrylic acid), Polymethacrylate and Other Acrylic Polymers     -   Poly(vinyl alcohol) (PVA) and Copolymers         -   Poly(vinyl alcohol) (PVA)         -   Poly(vinyl alcohol-co-ethylene) ethylene     -   Poly(vinylpyrrolidone) (PVP) and Copolymers     -   Polyelectrolytes         -   Poly(styrenesulfonate) (PSS) and Copolymers         -   Polyacrylamide (PAM)-based Polyelectrolytes         -   Poly(acrylic acid) (PAA), Sodium Salt         -   Poly(allylamine hydrochloride)         -   Poly(diallyldimethylammonium chloride) Solution         -   Poly(vinyl acid)         -   Miscellaneous—(1)     -   Cucurbit[n]uril Hydrate     -   Quaternary ammonium polymers     -   Carboxypolymethylene (carbomer)     -   Polyvinyl methyl ether-maleic anhydride (PVM-MA)     -   Carboxypolymethylene (carboxyvinyl polymer)     -   Polyvinyl methyl ether-maleic anhydride     -   Carboxymethylcellulose     -   Hydroxyethylcellulose and derivatives     -   Methylcellulose and derivatives     -   Other cellulose ethers         -   Ethylcellulose         -   Hydroxypropylcellulose     -   Sodium carboxymethylcellulose     -   Hydroxyethylcellulose and ethyl hydroxyethylcellulose     -   Natural water-soluble polymers: Starches, Sugars,         Polysaccharides, Agar, Alginates, Carrageenan, Furcellaran,         Casein and caseinates, Gelatin, Guar gum and derivatives, Gum         arabic, Locust bean gum, Pectin, Cassia gum, Fenugreek gum,         Psyllium seed gum, Tamarind gum, Tara gum, Gum ghatti, Gum         karaya, Gum tragacanth, Xanthan gum, Curdlan, Diutan gum, Gellan         gum, Pullulan, Scleroglucan (sclerotium gum)

PEGs are available with different geometries, including, but not limited to, the following:

-   -   Branched PEGs: have three to ten PEG chains emanating from a         central core group.     -   Star PEGs: have 10 to 100 PEG chains emanating from a central         core group.     -   Comb PEGs: have multiple PEG chains normally grafted onto a         polymer backbone.

Substance Details for embodiments, including, but not limited to, one or more or a combination of the following:

-   -   Soluble substance     -   Soluble organic solvent     -   Soluble polymer     -   Water soluble substance     -   Soluble substance separable with a membrane     -   Water soluble substance separable with a membrane     -   Water soluble organic solvent     -   Water soluble polymer     -   Organic solvent separable with a membrane     -   Polymer separable with a membrane     -   Soluble organic solvent separable with a membrane     -   Soluble polymer separable with a membrane     -   Large molecular weight water soluble organic solvent     -   Small molecular weight water soluble polymer     -   Non-volatile organic solvent     -   Low volatility organic solvent     -   High volatility organic solvent that is separable with a         membrane     -   Organic solvent with a molecular weight, including, but not         limited to, greater than 100 da or any of the following: 125 da,         or 150 da, or 175 da, or 200 da, or 225 da, or 250 da, or 275         da, or 300 da, or 325 da, or 350 da, or 375 da, or 400 da, or         425 da, or 450 da, or 475 da, or 500 da, or 525 da, or 550 da,         or 575 da, or 600 da     -   Polymer with a molecular weight, including, but not limited to,         greater than 100 da or greater than any of the following: 125         da, or 150 da, or 175 da, or 200 da, or 225 da, or 250 da, or         275 da, or 300 da, or 325 da, or 350 da, or 375 da, or 400 da,         or 425 da, or 450 da, or 475 da, or 500 da, or 525 da, or 550         da, or 575 da, or 600 da     -   Substance with a molecular weight, including, but not limited         to, greater than 100 da or greater than any of the following:         125 da, or 150 da, or 175 da, or 200 da, or 225 da, or 250 da,         or 275 da, or 300 da, or 325 da, or 350 da, or 375 da, or 400         da, or 425 da, or 450 da, or 475 da, or 500 da, or 525 da, or         550 da, or 575 da, or 600 da     -   Organic solvent with a hydration radius, including, but not         limited to, greater than 100 da, or greater than any of the         following: 125 da, or 150 da, or 175 da, or 200 da, or 225 da,         or 250 da, or 275 da, or 300 da, or 325 da, or 350 da, or 375         da, or 400 da, or 425 da, or 450 da, or 475 da, or 500 da, or         525 da, or 550 da, or 575 da, or 600 da     -   Polymer with a hydration radius, including, but not limited to,         greater than 100 da, or or greater than any of the following:         125 da, or 150 da, or 175 da, or 200 da, or 225 da, or 250 da,         or 275 da, or 300 da, or 325 da, or 350 da, or 375 da, or 400         da, or 425 da, or 450 da, or 475 da, or 500 da, or 525 da, or         550 da, or 575 da, or 600 da     -   Substance with a hydration radius, including, but not limited         to, greater than 100 da, or greater than any of the following:         125 da, or 150 da, or 175 da, or 200 da, or 225 da, or 250 da,         or 275 da, or 300 da, or 325 da, or 350 da, or 375 da, or 400         da, or 425 da, or 450 da, or 475 da, or 500 da, or 525 da, or         550 da, or 575 da, or 600 da

Use of Redox Battery

If desired a redox battery may be implemented into the process at a suitable place to generate electricity. Typically, the place where it is employed depends upon the specific system. Generally, if a redox battery is employed then it may be located across a heat exchanger. If a pressure retarded osmosis membrane is employed then a redox battery may be employed prior to or alternatively after such a membrane.

If employed, then the battery is typically selected from an ammonia, ammonium carbonate or ammonium bicarbonate redox battery. Such batteries will typically employ a suitable metal as the anode and the cathode. Such metals include, for example, copper, zinc, nickel, silver, lead, cobalt, and mixtures thereof. Copper may be particularly preferable for some applications. In this manner ammonia or ammonium may react with the metal at the anode to produce a water soluble complex cation. At the cathode the solution may be decomposed using, for example, low grade heat which causes a solid metal to deposit. DC electricity is generated by completing the circuit via connecting the electrodes with, for example, a wire. The electrodes may be periodically swapped to ensure the electrode in the oxidation solution does not become too depleted. Suitable batteries are described in, for example, Energy Environ. Sci., 2015, 8, 343 Zhang et al., “A thermally regenerative ammonia-based battery for efficient harvesting of low-grade thermal energy as electrical power.”

Further Electricity Generation Through Employing a Copper-Ammonium Carbonate, Bicarbonate Redox Battery Following PRO (FIG. 11D):

The diluted ammonia-carbon dioxide draw solution produced after PRO is transferred into a solution in contact with a copper electrode (can also be, for example, Zinc, Nickel, Silver, Lead, Cobalt). The ammonia species reacts (oxidation) with the copper electrode (anode) to form a water soluble complex cation. The solution is then transferred to the heat exchanger in Component 3 (either in a continuous or in a batch system), where another copper electrode (cathode) is present in solution. The solution is decomposed using low grade heat in the heat exchanger, causing solid copper (Cu.sub.(s)) to be deposited on the copper electrode/cathode (reduction). As the copper electrode in the complex ion formation solution is oxidized and the copper electrode in the heat exchange is reduced, DC electricity is generated by connecting the electrodes with, for example, wire, thereby forming a complete circuit. The electrodes may be periodically swapped between solutions to ensure the copper electrode in the oxidation solution does not become too depleted.

FIG. 11D depicts a diagram of the system wherein a novel regenerated copper-ammonium carbonate, bicarbonate battery is employed to generate additional electricity in the process. Copper is oxidized in the complex-ion formation solution and is reduced in the thermal decomposition solution (heat exchange), generating DC electricity. Copper solid is removed/depleted from the copper electrode in the Copper Oxidation solution and deposited on the copper electrode in the Copper Reduction solution. The electrodes may be switched between solutions periodically to ensure the copper electrode in the oxidation solution never becomes too depleted.

3. Electricity Generation from Employing a Copper-Ammonium Carbonate, Bicarbonate Redox Battery (Membrane-Free Process) (FIG. 12):

The ammonia-carbon dioxide solution produced in component 1 is transferred into a solution in contact with a copper electrode (can also be, for example, Zinc, Nickel, Silver, Lead, Cobalt). The ammonia species reacts (oxidation) with the copper electrode (anode) to form a water soluble complex cation. The solution is transferred to the heat exchanger in Component 3 (either in a continuous or in a batch system), where another copper electrode (cathode) is present in solution. The solution is decomposed using low grade heat in the heat exchanger, causing solid copper (Cu.sub.(s)) to be deposited on the copper electrode/cathode (reduction). As the copper electrode in the complex ion formation solution is oxidized and the copper electrode in the heat exchange is reduced, DC electricity is generated by connecting the electrodes with wire, forming a complete circuit. The electrodes may be periodically swapped between solutions to ensure the copper electrode in the oxidation solution never becomes too depleted.

FIG. 12 depicts a diagram of the system wherein a membrane-less variation of the system in FIG. 11D generates electricity and valuable nitrogen compounds. This variation of the system generates electricity with a regenerated copper-ammonium carbonate, bicarbonate battery, while advantageously continuing to produce an ammonia-carbon dioxide gas mixture at a suitable molar ratio for ammonium carbamate synthesis.

4. Further Electricity Generation Through Employing a Copper-Ammonium Carbonate, Bicarbonate Redox Battery Prior to PRO (FIG. 13).

FIG. 13 depicts a variation of the above systems that generates electricity and captures carbon dioxide. This variation of the system generates electricity with a regenerated copper-ammonium carbonate, bicarbonate battery, while capturing carbon dioxide using an aqueous semipermeable membrane.

PRO Effectiveness

As shown in FIG. 14, at an NH.sub.3:CO.sub.2 molar ratio of 1.5:1, the solution has a pH of about 9 at a temperature of 298K. Pressure retarded osmosis is generally effective when NH4+species are present. NH.sub.3(aq) (non-ionic species) often acts in a similar manner to water with most PRO membranes.

5. Electricity Generation Using Reverse Electro Dialysis (RED):

The ammonia-carbon dioxide species solution created in component 1 is used as a concentrated solution while the LC or de-ionized water solution regenerated in the integrated process is used as the opposing solution. The solutions are separated by stacked anion and cation exchange membranes (AEM and CEM). On the ends of the stack, there is an anode and a cathode. Electricity is generated when the net negative change produced by the AEM and the net positive charge produced by the CEM is neutralized by the anode and cathode in a DC circuit. Such methods are described in, for example, Paripati et al., US 20140026567 which is incorporated herein by reference.

6. Other Methods to Generate Electricity from Aqueous Concentration Gradients (e.g. CAPMIX):

There are other methods for generating electricity from concentration gradients, including capacitive mixing power production (CAPMIX). These methods include the use of Nano-Battery Electrodes (NBE), Capacitive Double Layer Expansion (CDLE), and/or Capacitors Charged by the Donnan Potentials (CDP). These methods are described in, for example, Energy Procedia, Volume 20, 2012, Pages 108-115 Technoport 2012—Sharing Possibilities and 2nd Renewable Energy Research Conference (RERC2012) CAPMIX—Deploying Capacitors for Salt Gradient Power Extraction; M. F. M. Bijmans, et al. which is incorporated herein by reference.

A process for separating carbon dioxide comprising: forming a first solution comprising a salt of carbonate, bicarbonate, carbamate, or a mixture thereof; and decomposing the first solution to form a second aqueous solution comprising ammonia, amine, carbon dioxide, a salt of carbonate, bicarbonate, carbamate or a mixture thereof; wherein the decomposing of the first solution to form said second aqueous solution is conducted in the presence of a solvent to form gaseous carbon dioxide; and then separating at least a portion of the solvent from the second aqueous solution. The integrated process further comprises employing an ammonia, ammonium carbonate, or ammonium bicarbonate redox battery with electrodes selected from the group consisting of copper, zinc, nickel, silver, lead, and cobalt. 

What is claimed is:
 1. A method of generating electricity from a carbon capture process comprising: reacting ammonia or an ammonium compound with a metal to form a complex cation solution at an anode electrode; decomposing the complex cation solution to deposit a metal at a cathode electrode; and connecting the electrodes to generate electricity; wherein the complex cation solution comprises captured carbon dioxide.
 2. The process of claim 1 wherein the electrodes are selected from the group consisting of: copper, zinc, nickel, silver, lead, and cobalt.
 3. The process of claim 1 wherein the complex cation solution comprises monoethanolamine, methylamine, dimethylamine and trimethylamine.
 4. The process of claim 1 wherein the electrodes are periodically swapped.
 5. The process of claim 1 wherein the process further comprises employing a membrane.
 6. The process of claim 5 wherein the membrane is selected from the group consisting of semi-permeable membranes, pressure retarded osmosis membranes, forward osmosis membranes, anion exchange membranes (AEM), and cation exchange membranes (CEM).
 7. The process of claim 1 further comprising capturing carbon dioxide from combustion, oxidation, steam reforming, a gas shift reaction, catalytic reforming, natural gas purification, land fill gas, biogas, waste water treatment, fermentation, respiration, air, or from a mixture thereof.
 8. The process of claim 1 further comprising using the electricity generated to produce a compound comprising nitrogen.
 9. The process of claim 8 wherein the compound comprising nitrogen is ammonium carbamate, urea, cyanuric acid, or a derivative thereof.
 10. The process of claim 1 further comprising desorbing carbon dioxide from the complex cation solution.
 11. The process of claim 1 wherein the cathode electrode and anode electrode are located across a heat exchanger.
 12. The process of claim 1 wherein the process further comprises employing a pressure retarded osmosis membrane prior to reacting ammonia or an ammonium compound with a metal to form a complex cation solution at an anode electrode.
 13. The process of claim 1 wherein the process further comprises employing a pressure retarded osmosis membrane subsequent to reacting ammonia or an ammonium compound with a metal to form a complex cation solution at an anode electrode.
 14. The process of claim 1 further comprising heating the complex cation solution.
 15. The process of claim 1 wherein the electrodes are copper.
 16. The process of claim 1 wherein the electrodes are connected with a wire to generate electricity.
 17. The process of claim 1 wherein the complex cation solution comprises ammonium carbonate, ammonium biocarbonate, or a mixture thereof.
 18. A battery comprising: an anode electrode; a cathode electrode; a wire connecting the anode electrode and cathode electrode; a complex cation solution comprising the reaction product of a metal, ammonia or an ammonium compound, and captured carbon dioxide wherein said complex cation solution is capable of being decomposed at the cathode electrode.
 19. The battery of claim 18 wherein the metal is copper.
 20. The battery of claim 18 wherein the complex cation solution comprises monoethanolamine, methylamine, dimethylamine and trimethylamine. 